CN102504080B - Dispersing agent for reusing reclaimed water prepared from production wastewater as circulating cooling water and preparation method - Google Patents
Dispersing agent for reusing reclaimed water prepared from production wastewater as circulating cooling water and preparation method Download PDFInfo
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- CN102504080B CN102504080B CN201110319851.9A CN201110319851A CN102504080B CN 102504080 B CN102504080 B CN 102504080B CN 201110319851 A CN201110319851 A CN 201110319851A CN 102504080 B CN102504080 B CN 102504080B
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Abstract
The invention discloses a dispersing agent for reusing reclaimed water prepared from production wastewater as circulating cooling water and a preparation method of the dispersing agent through a copolymerization method. The dispersing agent is a mixture with multiple active groups and produced by multi-component copolymerization reaction; calcium carbonate and calcium phosphate crystals and organic microparticles can be effectively prevented from forming deposited scale through the adsorption and chelation effects between the dispersing agent and inorganic scaling microcrystals in water, such as calcium carbonate and calcium phosphate as well as the organic microparticles; the dispersing agent specifically meets the characteristics that the reclaimed water obtained after wastewater treatment is high in hardness and high in base and contains multiple complex organic matters, and effectively takes good scale inhibition and dispersion effects on a circulating water system for reclaimed water recycling, thereby obtaining good and long-acting treatment effect.
Description
Technical field
The invention belongs to polymer high efficiency dispersion agent technical field, especially relate to water in a kind of factory effluent system and be back to dispersion agent and the preparation method of recirculated cooling water.
Background technology
Middle water reuse has huge environment and economic benefit, it is the modern technique of pure environmental protection, but enterprise's waste discharge is complicated different with treatment process because originating, after causing processing, water quality is different, water quality is severe, the feature that in after production wastewater treatment, water self has, can bring very ill effect to circulating water system, careless slightly, to have a strong impact on circulating water treatment effect, and then have a strong impact on the operation of production system, cause and stop production or equipment damage, the scope of application and the usage quantity of water reuse in serious restriction.
A lot of enterprises can adopt dispersion agent to carry out the micro substance containing in controlled circulation water system, but because trade effluent is in processing in water process, water quality is unstable, foreign ion is numerous, existing dispersion agent in industry is the micro substance in controlled circulation water system effectively, the serious scale and the corrosion that cause as phosphate radical, calcium ions and magnesium ions, basicity, chlorion and various flora and algae etc.
Summary of the invention
The technical problem to be solved in the present invention is to provide water in a kind of factory effluent system and is back to dispersion agent of recirculated cooling water and preparation method thereof.
In factory effluent system, water is back to a dispersion agent for recirculated cooling water, and its general structure is as follows:
Wherein: m represents that 1～150 natural number, n represent that 1～50 natural number, p represent that 1～100 natural number, x represent 1～100 natural number, and the molecular weight of above-claimed cpd is 1000～20000.
In above-mentioned factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, comprises the following steps, and wherein the dosage of each raw material all refers to parts by weight:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 30～36 parts of deionization water of productive use and 5～7.5 parts of Virahols are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 8～12 parts of MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 3～4 parts of methyl acrylates and 6～9 parts of vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 3～8 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 3～7 parts of AMPS and 15～18 parts of deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 2.5～3.0 parts of initiators and 15～18 parts of deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, bottoming liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 12～15 parts of isopropanol water solutions;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 12～15 parts of deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
Preferably, described initiator is the one in ammonium persulphate, Potassium Persulphate.
Preferably, in above-mentioned factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, comprises the following steps, and wherein the dosage of each raw material all refers to parts by weight:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 30～32 parts of deionization water of productive use and 6～7.5 parts of Virahols are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 10～12 parts of MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 3～3.5 parts of methyl acrylates and 6～7.5 parts of vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 3～8 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 3～5 parts of AMPS and 15～16 parts of deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 2.5～2.8 parts of initiators and 15～16 parts of deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, bottoming liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 12～14 parts of isopropanol water solutions;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 12～14 parts of deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
Advantage of the present invention and effect: this dispersion agent is that multi-component copolymer reaction generates the compounding substances with various active group, by with water in absorption, the sequestering action of the inorganic scaling microcrystal such as calcium carbonate, calcium phosphate and organic microparticle, can effectively stop calcium carbonate, calcium phosphate crystal and organic particle to form deposition dirt, the height that in meeting especially after wastewater treatment there is glassware for drinking water is hard, high-alkali and contain the organic feature of numerous complicated, effectively the circulating water system of centering water reuse plays good scale inhibition, dissemination, obtains good, long-acting treatment effect; And this dispersion agent can with inhibition, the scale inhibition agent good combination such as other organic carboxyl acid classes, solve middle water and be back to use incidental fouling, the etching problem in recirculated water process, for making water in numerous complicated can be back to use circulating cooling system, realize to greatest extent the object of saving water and energy.
Embodiment
In order to understand the present invention, below by specific embodiment, the invention will be further described.
In factory effluent system of the present invention, water is back to the dispersion agent of recirculated cooling water, and its general structure is:
Its preparation method is: appropriate vinylformic acid and AMPS, methyl acrylate, MALEIC ANHYDRIDE, under about 70 ℃ to 100 ℃ environment, under initiator exists, are carried out to copolymerization and made, and the chemical equation of copolyreaction is as follows:
Wherein, m represents that 1～150 natural number, n represent that 1～50 natural number, p represent that 1～100 natural number, x represent 1～100 natural number, and the molecular weight of above-claimed cpd is 1000～20000.
Embodiment mono-:
In factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, comprises the following steps:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 300kg deionization water of productive use and 75kg Virahol are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 115kg MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 32kg methyl acrylate and 66kg vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 5 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 43kgAMPS and 150kg deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 26kg ammonium persulphate and 150kg deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, bottoming liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 120kg isopropanol water solution;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 120kg deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
Products obtained therefrom is the aqueous solution that the massfraction of solid matter is 30%, as analyzes the too high amount that can increase deionization water of productive use of rear product effective content, is adjusted into 30% rear use.
Embodiment bis-:
In factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, comprises the following steps:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 360kg deionization water of productive use and 75kg Virahol are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 120kg MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 40kg methyl acrylate and 90kg vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 6 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 70kgAMPS and 180kg deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 30kg Potassium Persulphate and 180kg deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, end liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 150kg isopropanol water solution;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 150kg deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
Products obtained therefrom is the aqueous solution that the massfraction of solid matter is 30%, as analyzes the too high amount that can increase deionization water of productive use of rear product effective content, is adjusted into 30% rear use.
Embodiment tri-:
In factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, comprises the following steps:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 300kg deionization water of productive use and 50kg Virahol are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 80kg MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 30kg methyl acrylate and 60kg vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 3 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 30kgAMPS and 150kg deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 25kg initiator and 150kg deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, end liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 130kg isopropanol water solution;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 130kg deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
Products obtained therefrom is the aqueous solution that the massfraction of solid matter is 30%, as analyzes the too high amount that can increase deionization water of productive use of rear product effective content, is adjusted into 30% rear use.
In all embodiment of the present invention, described initiator is the one in ammonium persulphate, Potassium Persulphate.
The effect of dispersion agent of the present invention is verified by the dynamic anti-scale distributed test of following testing laboratory:
Test method: under same water quality, add the medicament that contains different dispersion agents, move at laboratory simulation actual cycle cooling system working condition by dynamic analog device, heat exchange tube wall heat transfer conditions in simulation interchanger in the Mobile state of going forward side by side monitoring, computing system, it is fouling resistance, investigate the scale inhibition dispersion effect of dispersion agent
Test water is water in certain enterprise's typical production, and in test, water water quality is as follows:
| Numbering | Project | Unit | Numerical value |
| 1 | pH | 7.5 | |
| 2 | Calcium ion | Mg/L is (with CaCO 3Meter) | 100 |
| 3 | Magnesium ion | Mg/L is (with CaCO 3Meter) | 120 |
| 4 | Total hardness | Mg/L is (with CaCO 3Meter) | 320 |
| 5 | Total alkalinity | Mg/L is (with CaCO 3Meter) | 200 |
| 6 | COD | mg/L | 40 |
| 7 | Phosphate radical | mg/L | 5 |
Test medicine, adopts and adds equivalent organic phosphoric acid and the different types of dispersion agent 30mg/L of equivalent, controls concentrated 3 times, moves after 72 hours, calculates fouling resistance, the Mobile state scale inhibition simultaneous test of going forward side by side, and test-results is as follows:
National standard, fouling resistance is less than 3.44 × 10
-4m
2k/W
Can be found out by above test, novel dispersant is compared with existing common binary, terpolymer, and water in typical case is back to use after circulating water system, greatly reduces fouling resistance, improve heat exchange efficiency, had better scale inhibition dispersion effect than current common binary, terpolymer.
The present invention is not limited to above-mentioned preferred forms, and other any or akin products identical with the present invention that anyone draws under enlightenment of the present invention, within all dropping on protection scope of the present invention.
Claims (3)
1. in factory effluent system, water is back to the preparation method of the dispersion agent of recirculated cooling water, it is characterized in that: the general structure of prepared dispersion agent is as follows:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 30～36 parts of deionization water of productive use and 5～7.5 parts of Virahols are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 8～12 parts of MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 3～4 parts of methyl acrylates and 6～9 parts of vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 3～8 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 3～7 parts of AMPS and 15～18 parts of deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 2.5～3.0 parts of initiators and 15～18 parts of deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, bottoming liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 12～15 parts of isopropanol water solutions;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 12～15 parts of deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
2. water is back to the preparation method of the dispersion agent of recirculated cooling water in factory effluent system as claimed in claim 1, it is characterized in that: described initiator is the one in ammonium persulphate, Potassium Persulphate.
3. water is back to the preparation method of the dispersion agent of recirculated cooling water in factory effluent system as claimed in claim 1, it is characterized in that: comprise the following steps, wherein the dosage of each raw material all refers to parts by weight:
1) preparation of raw material with add
A. bottoming liquid is prepared and is added: first 30～32 parts of deionization water of productive use and 6～7.5 parts of Virahols are passed through in vacuum pump sucting reaction still successively, make in reactor more than liquid level is positioned at the minimum level of stirring, then add 10～12 parts of MALEIC ANHYDRIDE from reactor ingress, open and stir, under normal temperature, be stirred to solid material and fully dissolve;
B.1 number monomer solution preparation: 3～3.5 parts of methyl acrylates and 6～7.5 parts of vinylformic acid are sucked respectively in No. 1 header tank by vacuum pump, suck after two kinds of raw materials, then vacuumize 3～8 minutes, two kinds of raw materials are mixed, form No. 1 monomer solution;
C.2 number monomer solution preparation: 3～5 parts of AMPS and 15～16 parts of deionization water of productive use are put into weighing bucket, be stirred to dissolution of solid and mix No. 2 monomer solutions of rear formation, No. 2 monomer solutions are sucked in No. 2 header tanks with vacuum pump; Wherein AMPS refers to 2-acrylamide-2-methyl propane sulfonic;
D. the preparation of initiator solution: 2.5～2.8 parts of initiators and 15～16 parts of deionization water of productive use are joined in weighing bucket, after being stirred to dissolution of solid and mixing, form initiator solution, initiator solution is drawn in No. 3 header tanks with vacuum pump;
2) copolyreaction
A. open the agitator of reactor, close by-pass valve under condenser, in reacting kettle jacketing, pass into 1～2kg/cm
2steam, bottoming liquid in reactor is heated to 70 ℃, open the bottom valve of No. 3 header tanks, the initiator solution of 1/2nd in No. 3 header tanks is added drop-wise in reactor fast, in dripping, monitor temperature of charge, rate of addition and bottoming liquid temp steady that keeps initiator solution, adds after the initiator solution of 1/2nd in No. 3 header tanks, closes the bottom valve of No. 3 header tanks;
B. reactor temperature is raised to 80～85 ℃, then stop heating, vapour condensation water in chuck is all emitted, No. 1 header tank of synchronous unlatching, the bottom valve of No. 2 header tanks and No. 3 header tanks, by No. 1 monomer solution, No. 2 monomer solutions splash in reactor with the initiator solution of residue 1/2nd, keep rate of addition stable, the time for adding of No. 1 monomer solution and No. 2 monomer solutions was controlled in 3 hours, the initiator solution of residue 1/2nd is later than No. 1 monomer solution and No. 2 monomer solutions complete for 5 minutes, and in whole dropping process, temperature in reactor is lower than 95 ℃,
C.1 after number monomer solution, No. 2 monomer solutions and initiator solution are all added dropwise to complete, open by-pass valve under condenser, strengthen chuck inner vapor flow, making reactor temperature is 90～100 ℃, steams 12～14 parts of isopropanol water solutions;
After the distillation of d.c step finishes, in the chuck of reactor, pass into water coolant, the temperature in reactor is dropped to below 60 ℃, add 12～14 parts of deionization water of productive use, stop stirring and cooling, now, in reactor, copolyreaction completes, and generates feed liquid;
E. the feed liquid that in reactor, copolyreaction generates, after stainless steel filtering net, the two-layer filtration of absorbent cotton, weighs and packs.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201110319851.9A CN102504080B (en) | 2011-10-20 | 2011-10-20 | Dispersing agent for reusing reclaimed water prepared from production wastewater as circulating cooling water and preparation method |
Applications Claiming Priority (1)
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