CN203602538U - System for reducing consumption of hydrochloric acid and calcium chloride during production of sodium alginate - Google Patents
System for reducing consumption of hydrochloric acid and calcium chloride during production of sodium alginate Download PDFInfo
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- CN203602538U CN203602538U CN201320852696.1U CN201320852696U CN203602538U CN 203602538 U CN203602538 U CN 203602538U CN 201320852696 U CN201320852696 U CN 201320852696U CN 203602538 U CN203602538 U CN 203602538U
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Abstract
The utility model discloses a system for reducing the consumption of hydrochloric acid and calcium chloride during production of sodium alginate. The system comprises a calcification tank, an aging pool, a first-stage decalcification tank, a first-stage draining stranding cage, a second-stage decalcification tank, a second-stage draining stranding cage, a third-stage decalcification tank, a third-stage draining stranding cage and a screw press dehydrator which are connected with one another in sequence, wherein a waste acid water outlet of the second-stage draining stranding cage is connected with the first-stage decalcification tank and the calcification tank through a second-stage storage tank; the waste acid water outlet of the first-stage draining stranding cage is connected with the calcification tank through a first-stage storage tank; the waste acid water outlet of the third-stage draining stranding cage is connected with the calcification tank through a third-stage storage tank; the screw press dehydrator is connected with the calcification tank through a press storage tank. By adopting the system disclosed by the utility model reduces the consumption of calcium chloride required by a calcification reaction, and saves the consumption of hydrochloric acid required by the adjustment of the PH value of the calcification tank and required by the first-stage decalcification.
Description
Technical field
The utility model relates to seaweed chemical production technical field, particularly relates to a kind of chlorination of hydrochloric acid calcium consumption systems in sodium alginate production that reduces.
Background technology
In seaweed chemical industry, sodium alginate solution after flotation is filtered, adds suitable mineral acid or calcium chloride, makes water miscible sodium alginate change water-insoluble alginic acid or calcium alginate into and the concentrated process of separating out is called cohesion, the former is called acidization, and the latter is called calcification.Cohesion is an important refining and enrichment process in sodium alginate technique.
The advantages such as because calcification yield generally improves 10% left and right than acidization, and the fibrous tissue of the calcium alginate gel producing is tough and tensile, and flexible and dehydration is convenient, thereby from the nineties in last century, the domestic same industry is eliminated acidization gradually, makes calcification into.Through the development of recent two decades, calcification technique is ripe gradually, but hydrochloric acid, the general higher problem of calcium chloride consumption exists always, and industry consumes common level and is: hydrochloric acid 1.75t/t, solid calcium chloride 1.5t/t.
In the production of calcification sodium alginate, calcification operation comprises calcification cohesion and two technological processs of hydrochloric acid decalcification.
1, calcify reaction
Reaction equation: 2NaAlg+Cacl
2=CaAlg+2Nacl;
The side reaction that may exist: Na
2cO
3+ Cacl
2=CaCO
3+ 2Nacl
Calcify reaction makes water miscible sodium alginate become water-insoluble calcium alginate to separate out, and in sodium alginate solution, the impurity such as great amount of soluble inorganic salt and pigment is also got rid of with water simultaneously.
Although sodium alginate is very easily got off by precipitated cationics more than most of two valencys, owing to containing the Na of surplus in sodium alginate solution
2cO
3, and showing slightly alkalescence, PH is generally between 10.0-10.5.For avoiding generating precipitation of calcium carbonate in the process of calcify reaction, generally in calcium chloride solution, add hydrochloric acid to be made into acid chlorization calcium, in calcium liquid, hydrogen chloride content is 25-30 grams per liter, and the PH=7.0 while making to react is as the criterion, and is also that the waste Ca water that discharge in aging pond should show neutral.
For making calcify reaction complete, need to keep the concentration of the calcium ion of ionic equilibrium to be generally not less than 0.045%.
2, decalcification reaction
Reaction equation: CaAlg+2Hcl=2HAlg+2Cacl
2;
In production, be generally divided into three grades of decalcifications.One-level decalcification adds a small amount of hydrochloric acid, regulates PH=1.5-2.0; Secondary decalcification adds enough hydrochloric acid; Three grades of decalcifications claim again washing, add quantitative tap water, the hydrochloric acid of wash residual.Waste water after decalcifications at different levels is directly disposed to environmental protection station processing together with squeezing the waste water (being referred to as below decalcification waste acid water) of deviating from.
Making into after calcification from acidization, in view of there being the impurity such as some pigments in decalcification waste acid water, for not affecting quality product, is all that it is directly disposed to environmental protection treatment in industry.For many years, never find suitable way to recycle.
Summary of the invention
The purpose of this utility model is exactly that a kind of chlorination of hydrochloric acid calcium consumption systems in sodium alginate production that reduces is provided for the defect of above-mentioned existence.The utility model changes the part technical process of calcification operation, by H
+the secondary decalcification waste acid water that concentration is higher returns to one-level decalcification tank or calcification tank, replaces hydrochloric acid to use as decalcification at one-level decalcification tank; By H
+decalcification waste acid water is returned to calcification tank by one-level decalcification waste acid water that concentration is lower, three grades of decalcification waste acid waters, squeezing waste acid water etc., makes Ca wherein
2+participate in calcify reaction, keep the necessary ionic equilibrium concentration of reaction; Make H wherein
+regulate calcium chloride to make it aobvious acid, keep the waste Ca water PH=7 discharging.So both reclaimed the Ca that hydrochloric acid elutes
2+, reclaimed again remaining H wherein
+thereby, reduce the needed calcium chloride consumption of calcify reaction, save adjusting calcium chloride and be acidity and the needed hydrochloric acid consumption of one-level decalcification.Realize thus three grades of gradient utilizations of hydrochloric acid, formed the advanced technologies of calcium ion and the whole recycles of acid ion in decalcification waste acid water.Because pigment, water-soluble impurity etc. in decalcification waste acid water are all along with waste Ca water is discharged, thereby can not have any impact to quality product.
Of the present utility model a kind of reduce sodium alginate produce in chlorination of hydrochloric acid calcium consumption systems technical scheme be to comprise the calcification tank connecting successively, aging pond, one-level decalcification tank, one-level draining cage, secondary decalcification tank, secondary draining cage, three grades of decalcification tanks, three grades of draining cages, spiral pressing dehydrator;
The waste acid water outlet of secondary draining cage is connected with one-level decalcification tank and calcification tank by secondary basin; The waste acid water outlet of one-level draining cage is connected with calcification tank by one-level basin; The waste acid water outlet of three grades of draining cages connects calcification tank by three grades of basins; Spiral pressing dehydrator connects calcification tank by squeezing basin.
Between secondary basin and one-level decalcification tank and calcification tank, be provided with secondary fluorine alloy pump.
One-level basin with between be provided with one-level fluorine alloy pump and be connected.
Between three grades of basins and calcification tank, be provided with three grades of fluorine alloy pumps.
Squeezing basin connects calcification tank by squeezing fluorine alloy pump.
The decalcification waste acid water of secondary draining cage higher concentration is entered to secondary basin, be pumped to one-level decalcification tank and/or calcification tank with secondary fluorine alloy, the decalcification waste acid water of one-level draining cage lower concentration is entered to one-level basin, be pumped to calcification tank with one-level fluorine alloy, the decalcification waste acid water of three grades of lower concentration draining cages is entered to three grades of basins, be pumped to calcification tank with three grades of fluorine alloy, the decalcification waste acid water of spiral pressing dehydrator lower concentration is drained into squeezing basin, be pumped to calcification tank with squeezing fluorine alloy.
The beneficial effects of the utility model are: decalcification waste acid water is returned to calcification tank by the utility model, make Ca wherein
2+participate in calcify reaction, keep the necessary ionic equilibrium concentration of reaction; Make H+ wherein regulate calcium chloride to make it aobvious acid, keep the waste Ca water PH=7 discharging.So both reclaimed the Ca that hydrochloric acid elutes
2+, reclaim again remaining H+ wherein, thereby reduced the needed calcium chloride consumption of calcify reaction, save adjusting calcium chloride and be acid needed hydrochloric acid consumption.Formed thus the advanced technologies of calcium ion and the whole recycles of acid ion in decalcification waste acid water, reduce sodium alginate produce in hydrochloric acid, calcium chloride consumption.Because pigment, water-soluble impurity etc. in decalcification waste acid water are all along with waste Ca water is discharged, thereby can not have any impact to quality product.
The utility model, on the basis of great many of experiments, by changing the part flow process of calcification operation in sodium alginate production, makes the Ca in factory effluent
2+and H
+obtain recycle, sodium alginate per ton is saved technical hydrochloric acid (technical hydrochloric acid content 30%) 0.657 ton, saves solid calcium chloride and (refers to CaCl
22H
2o) 0.232 ton, two consumption indicators are all recorded lower than document.Ton production cost reduces by 373 yuan, and by producing 5000 tons of calculating per year, year increases benefit more than 180 ten thousand yuan.
accompanying drawing explanation:
Figure 1 shows that prior art processes schema;
Figure 2 shows that the utility model process flow sheet.
Wherein, 1-calcification tank, the aging pond of 2-, 3-one-level decalcification tank, 4-one-level draining cage, 5-secondary decalcification tank, 6-secondary draining cage, tri-grades of decalcification tanks of 7-, tri-grades of draining cages of 8-, 9-spiral pressing dehydrator, 10-one-level fluorine alloy pump, 11-one-level basin, 12-secondary fluorine alloy pump, 13-secondary basin, tri-grades of fluorine alloy pumps of 14-, tri-grades of basins of 15-, 16-squeezing fluorine alloy pump, 17-squeezes basin.
embodiment:
In order to understand better the utility model, describe the technical solution of the utility model in detail with specific examples below.
A kind of chlorination of hydrochloric acid calcium consumption systems in sodium alginate production that reduces of the present utility model, be divided into calcification operation and decalcification operation, comprise calcification tank 1, aging pond 2, one-level decalcification tank 3, one-level draining cage 4, one-level fluorine alloy pump 10, one-level basin 11, secondary decalcification tank 5, secondary draining cage 6, secondary fluorine alloy pump 12, secondary basin 13, three grades of decalcification tanks 7, three grades of draining cages 8, three grades of fluorine alloy pumps 14, three grades of basins 15, spiral pressing dehydrator 9, squeezing fluorine alloy pump 16, squeezing basin 17; The decalcification waste acid water of secondary draining cage 6 higher concentration is entered to secondary basin 13, deliver to one-level decalcification tank 3 and/or calcification tank 1 with secondary fluorine alloy pump 12, the decalcification waste acid water of one-level draining cage 4 lower concentration is entered to one-level basin 11, deliver to calcification tank 1 with one-level fluorine alloy pump 10, the decalcification waste acid water of three grades of lower concentration draining cages 8 is entered to three grades of basins 15, deliver to calcification tank 1 with three grades of fluorine alloy pumps 14, the decalcification waste acid water of spiral pressing dehydrator lower concentration 9 is drained into squeezing basin 17, deliver to calcification tank 1 with squeezing fluorine alloy pump 16.
In embodiment, relate to the method for inspection:
Ca
2+the method of inspection: EDTA volumetry.
H
+the method of inspection: acid base titration.
In the sodium alginate production of prior art, chlorination of hydrochloric acid calcium consumes:
Equipment:
In Shandong Jie Jing group, two glue workshop calcification operations are carried out.Comprise calcification tank 1, aging pond 2, one-level decalcification tank 3, one-level draining cage 4, secondary decalcification tank 5,7, three grades of draining cages 8 of 6, three grades of decalcification tanks of secondary draining cage, spiral pressing dehydrator 9, specifically asks for an interview Figure of description: Fig. 1.
Implementation process: by Ca
2+the calcium chloride solution of content 4.685% is made into acidity, adds the hydrochloric acid preparation of 25 gram 30% by every liter of calcium chloride solution.
The sodium alginate solution of last operation is delivered to calcification tank 1 and carry out calcify reaction, add acid chlorization calcium solution, regulate aging pond 2 water outlet PH=7.0, water-soluble sodium alginate solution is become to water-insoluble calcium alginate throw out.
The interior calcium alginate in aging pond 2 is sent into one-level decalcification tank 3, add appropriate hydrochloric acid, between the interior PH=2.5-3.0 of regulating tank.Calcium alginate, after one-level decalcification tank 3 carries out partly decalcifying reaction, enters one-level draining cage 4, and the one-level decalcification waste acid water that drop goes out drains into environmental protection, and material (comprising calcium alginate and alginic acid) enters secondary decalcification tank 5.
In secondary decalcification tank 5, add enough hydrochloric acid, between the interior PH=1.5-2.0 of regulating tank.Material fully carries out, after decalcification reaction, entering secondary draining cage 6 at secondary decalcification tank 5, and the secondary decalcification waste acid water that drop goes out drains into environmental protection, and material (comprising a small amount of calcium alginate and most alginic acid) enters three grades of decalcification tanks 7.
In three grades of decalcification tanks 7, add appropriate tap water, between the interior PH=2.0-2.5 of regulating tank.Material is proceeded decalcification reaction at three grades of decalcification tanks 7, and washes most Ca off by tap water
2+and H
+after, entering three grades of draining cages 8, three grades of decalcification waste acid waters that drop goes out drain into environmental protection, and material (calcium alginate of alginic acid and denier) enters spiral pressing dehydrator 9.
Material after spiral pressing dehydrator 9 dehydration, in and operation add Na
2cO
3reaction generates sodium alginate, then is finished product sodium alginate by baking operation oven dry.The waste acid water that squeezing is taken off also drains between environment-friendly vehicle.
Finally obtain 1.15 tons of sodium alginates, consumption liquid calcium chloride 9.775m
3(ton consumption 8.50 m
3), 0.125 ton of one-level decalcification tank consumption hydrochloric acid (0.11 ton of ton consumption), 1.038 tons of secondary decalcification tank consumption hydrochloric acid 1.194(ton consumptions), three grades of decalcification tank consumption tap water 46 m
3(ton consumption 40 m
3), discharge altogether waste Ca water 810 m
3(ton consumption 705 m
3).
Experimental data
Through embodiment 1 actual production decalcification waste acid water is carried out to inspection by sampling, show that experimental data is in Table: the table 1(decalcification spent acid water yield: refer to the amount that ton product produces);
Table 1
Said process is carried out to hydrochloric acid, calcium chloride material balance.
Calcium chloride:
Add: 4.685% × 8.5 × 111/40/0.755=1.464;
Discharge: (4.5 × 10
-4× 705+22 × 8.2 × 10
-4+ 1.3 × 10
-3× 23+32 × 5.4 × 10
-4+ 5 × 3.3 × 10
-4) × 111/40/0.755=1.412
Checking: substantially identical above, error is verify error, and after press dewatering in alginic acid few calcium ion do not count.
Hydrochloric acid:
Add: acidifying calcium chloride needs hydrochloric acid=8.5 × 25/1000/0.3=0.708, when decalcification, consume hydrochloric acid 1.038+0.11=1.148, add up to 1.856 tons.
Discharge: the hydrochloric acid of acidifying calcium chloride is discharged regulate PH in waste Ca water after, therefore be also 0.708 ton, decalcification consumptions at different levels acid=(22 × 1.92 × 10
-5+ 1.56 × 10
-4× 23+32 × 4.93 × 10
-5+ 5 × 5.73 × 10
-5) × 36.5/0.3=0.715, the alginic acid that generates 2.45 tons moisture 72% needs hydrochloric acid 2.45 × 28%/194 × 36.5/0.3=0.43.
Discharge hydrochloric acid total=0.708+0.715+0.43=1.853 ton, coincide with the hydrochloric acid content adding.
According to above-mentioned material balance also as seen from table, in the decalcification waste acid water of draining, contain 0.247 ton, calcium chloride, 0.715 ton of hydrochloric acid.
Make into after calcification from acidization, although contain calcium chloride, hydrochloric acid in decalcification waste acid water, but in view of wherein there being the impurity such as some pigments, for not affecting quality product (whiteness, transparency), for many years, be all that it is directly disposed to environmental protection treatment, never find suitable way to recycle.
In sodium alginate production of the present utility model, chlorination of hydrochloric acid calcium consumes:
Equipment:
Calcification operation after Shandong Jie Jing group two glue shops is carried out.Comprise calcification tank 1, aging pond 2, one-level decalcification tank 3, one-level draining cage 4, secondary decalcification tank 5, secondary draining cage 6,7, three grades of draining cages 8 of three grades of decalcification tanks, spiral pressing dehydrator 9, one-level fluorine alloy pump 10, one-level basin 11, secondary fluorine alloy pump 12,14, three grades of basins 15 of 13, three grades of fluorine alloy pumps of secondary basin, squeezing fluorine alloy pump 16, squeezing basin 17.
Wherein, the one-level decalcification waste acid water that one-level draining cage 4 drops go out enters one-level basin 11, delivers to calcification tank 1 through one-level fluorine alloy pump 10; The secondary decalcification spent acid that secondary draining cage 6 drops go out enters secondary basin 13, delivers to one-level decalcification tank 3 and/or calcification tank 1 through secondary fluorine alloy pump 12; Three grades of decalcification waste acid waters that three grades of draining cage 8 drops go out enter three grades of basins 15, deliver to calcification tank 1 through three grades of fluorine alloy pumps 14; The decalcification waste acid water of spiral pressing dehydrator 9 enters squeezing basin 17, delivers to calcification tank 1 through squeezing fluorine alloy pump 16.Specifically ask for an interview Figure of description: Fig. 2.Newly added equipment particular sheet is in Table: table 2
Table 2
Implementation process:
The sodium alginate solution of last operation is delivered to calcification tank 1 and carry out calcify reaction, add Ca
2+the acid chlorization calcium solution of content 4.685%, regulates aging pond 2 water outlet PH=7.0, and water-soluble sodium alginate solution is become to water-insoluble calcium alginate throw out.
The interior calcium alginate in aging pond 2 is sent into one-level decalcification tank 3, add appropriate hydrochloric acid, between the interior PH=2.5-3.0 of regulating tank.Calcium alginate is after one-level decalcification tank 3 carries out partly decalcifying reaction, enter one-level draining cage 4, the one-level decalcification waste acid water that drop goes out drains into one-level basin 11, deliver to calcification tank 1 through one-level fluorine alloy pump 10, the aging pond 2PH of auxiliary adjustment, suitably turn down calcium chloride valve and join the hydrochloric acid valve in calcium chloride, material (comprising calcium alginate and alginic acid) enters secondary decalcification tank 5.
In secondary decalcification tank 5, add enough hydrochloric acid, between the interior PH=1.5-2.0 of regulating tank.Material fully carries out after decalcification reaction at secondary decalcification tank 5, enter secondary draining cage 6, the secondary decalcification waste acid water that drop goes out drains into secondary basin 13, delivers to one-level decalcification tank 3 or calcification tank 1 through secondary fluorine alloy pump 12, regulate one-level decalcification tank 3PH qualified, one-level decalcification tank 3 hydrochloric acid are turned off.Material (comprising a small amount of calcium alginate and most alginic acid) enters three grades of decalcification tanks 7.
In three grades of decalcification tanks 7, add appropriate tap water, between the interior PH=2.0-2.5 of regulating tank.Material is proceeded decalcification reaction at three grades of decalcification tanks 7, and washes most Ca off
2+and H
+after, entering three grades of draining cages 8, three grades of decalcification waste acid waters that drop goes out drain into three grades of basins 15, deliver to calcification tank 1 through three grades of fluorine alloy pumps 14, and the aging pond 2PH of auxiliary adjustment, suitably turns down calcium chloride valve, and the hydrochloric acid that regulates calcium chloride acidity is closed.Material (calcium alginate of alginic acid and denier) enters spiral pressing dehydrator 9.
Material after spiral pressing dehydrator 9 dehydration, in and operation add Na
2cO
3reaction generates sodium alginate, then is finished product sodium alginate by baking operation oven dry.The waste acid water that squeezing is taken off also drains into squeezing basin 17, delivers to calcification tank 1 through squeezing fluorine alloy pump 16, in order to regulate aging pond 2PH, suitably turns down calcium chloride valve.
So far, calcification operation completes start operation, and system is in stablizing normal operating condition.Now, only add hydrochloric acid at secondary decalcification tank 5, other is again without the place of the hydrochloric acid of annotating.After calcification process operations completes, decalcification waste acid waters at different levels are stayed in basins at different levels, treat that next class is used, therefore next class also no longer needs to regulate calcium chloride acidity with hydrochloric acid, no longer need in one-level decalcification tank 3, add again hydrochloric acid.
Finally obtain 1.235 tons of sodium alginates, consumption liquid calcium chloride 8.77m
3(ton consumption 7.10 m
3), just start to regulate 0.073 ton of hydrochloric acid of calcium chloride acidity (0.059 ton of ton consumption) one-level decalcification tank 3 to consume 0.013 ton of hydrochloric acid (0.01 ton of ton consumption), secondary decalcification tank 5 consumes hydrochloric acid 1.432(ton and consumes 1.16 tons), three grades of decalcification tanks 7 consume tap water 53m
3(ton consumption 43 m
3), discharge altogether waste Ca water 878 m
3(ton consumption 711 m
3).
The rear decalcification waste acid water content volumes at different levels of embodiment 2 are in Table: table 3.
Table 3
The experimental data of embodiment 2 is carried out to material balance:
Calcium chloride:
Add: 4.685% × 7.1 × 111/40/0.755=1.223;
Discharge: 4.5 × 10
-4× 711 × 111/40/0.755=1.176
Checking: due to the Ca of decalcification waste acid waters at different levels
2+all be recycled utilization, the calcium chloride amount therefore adding at calcification tank 1 obviously reduces, the 8.5m of origin
3reduce to 7.1 m
3.And the Ca discharging
2+all in waste Ca water, discharge no longer outer row Ca in decalcification waste acid waters at different levels
2+.The above results is substantially identical, and error is still verify error, and after press dewatering in alginic acid few calcium ion do not count.
Hydrochloric acid:
Add: in the time of just start, need acidifying calcium chloride to adjust aging pond 2PH, 0.059 ton of consumption hydrochloric acid (will no longer need hydrochloric acid while later normally production herein).
One-level decalcification tank 3 consumes hydrochloric acid: 0.01 ton (when normal production later, will no longer need hydrochloric acid herein).
The hydrochloric acid adding at secondary decalcification tank 5: 1.16 tons, 1.229 tons of above totals.
Discharge: the hydrochloric acid of acidifying calcium chloride is discharged regulate PH in waste Ca water after, therefore be 0.059 ton, decalcifications at different levels are discharged in decalcification waste acid water containing acid=(24 × 1.79 × 10
-5+ 1.58 × 22.5 × 10
-4+ 31 × 4.8 × 10
-5+ 6.5 × 5.55 × 10
-5) × 36.5/0.3=0.709, the alginic acid that generates 2.3 tons moisture 72% needs hydrochloric acid 2.6 × 28%/194 × 36.5/0.3=0.45.
Total=0.709+0.45+0.059=1.218 ton, coincide with the amount adding.
Know according to the material balance in embodiment 1, acidifying calcium chloride needs 0.708 ton of hydrochloric acid, and in the decalcification waste acid waters at different levels of draining hydrochloric 0.715 ton, substantially equal.In theory, if it is recycled to calcification tank 1 by all decalcification waste acid waters at different levels, the hydrochloric acid of acidifying calcium chloride will save.
Known by the material balance in embodiment 2, decalcification waste acid waters at different levels are all recycled to after calcification tank 1, acidifying calcium chloride no longer needs extra finished product technical hydrochloric acid to regulate, and produces the result of checking and the material balance of embodiment 1 is very identical by embodiment 2.Save thus the needed hydrochloric acid of the acid aging pond PH=7 of assurance of adjusting calcium chloride.Meanwhile, the add-on of calcification tank 1 calcium chloride is also by 8.5m
3reduce to 7.1m
3.
Consumption data of the present utility model is in Table: table 4.
Table 4
Through above-mentioned workflow reengineering, by H
+the secondary decalcification waste acid water that concentration is higher returns to one-level decalcification tank 3, replaces hydrochloric acid to use as decalcification at one-level decalcification tank 3; By H
+one-level decalcification waste acid water that concentration is lower, three grades of decalcification waste acid waters, squeezing waste acid water etc. return to calcification tank 1, make Ca wherein
2+participate in calcify reaction, keep the necessary ionic equilibrium concentration of reaction; Make H wherein
+regulate aging pond 2PH, keep the waste Ca water PH=7 discharging.So both reclaimed the Ca that hydrochloric acid elutes
2+, reclaimed again remaining H wherein
+thereby, reduce the needed calcium chloride consumption of calcify reaction, save adjusting calcium chloride and be acidity and the needed hydrochloric acid consumption of one-level decalcification.
Realize thus three grades of gradient utilizations of hydrochloric acid, formed the advanced technologies of calcium ion and the whole recycles of acid ion in decalcification waste acid water.
Because pigment, water-soluble impurity etc. in decalcification waste acid water are all along with waste Ca water is discharged, thereby can not have any impact to quality product.Implement the impact of front and back on quality product for checking the utility model, on production line, with same raw material, in the situation that other processing condition are identical, carried out contrast experiment, the results are shown in Table: table 5.As seen from table, the utility model implements quality product not affect.
Table 5
More than relate to the method for inspection:
Whiteness: spectrum diffuse-reflectance method.
Transparency: spectrophotometry.
As can be seen here, adopt the utility model to reduce hydrochloric acid, calcium chloride consumption, feasible in practice, investment is few, remarkable benefit.
Claims (5)
1. one kind is reduced chlorination of hydrochloric acid calcium consumption systems in sodium alginate production, it is characterized in that, comprise successively the calcification tank connecting, aging pond, one-level decalcification tank, one-level draining cage, secondary decalcification tank, secondary draining cage, three grades of decalcification tanks, three grades of draining cages, spiral pressing dehydrator;
The waste acid water outlet of secondary draining cage is connected with one-level decalcification tank and calcification tank by secondary basin; The waste acid water outlet of one-level draining cage is connected with calcification tank by one-level basin; The waste acid water outlet of three grades of draining cages connects calcification tank by three grades of basins; Spiral pressing dehydrator connects calcification tank by squeezing basin.
2. a kind of chlorination of hydrochloric acid calcium consumption systems in sodium alginate production that reduces according to claim 1, is characterized in that, is provided with secondary fluorine alloy pump between secondary basin and one-level decalcification tank and calcification tank.
According to claim 1 a kind of reduce sodium alginate produce in chlorination of hydrochloric acid calcium consumption systems, it is characterized in that, one-level basin with between be provided with one-level fluorine alloy pump and be connected.
According to claim 1 a kind of reduce sodium alginate produce in chlorination of hydrochloric acid calcium consumption systems, it is characterized in that, between three grades of basins and calcification tank, be provided with three grades of fluorine alloy pumps.
5. a kind of chlorination of hydrochloric acid calcium consumption systems in sodium alginate production that reduces according to claim 1, is characterized in that, squeezing basin connects calcification tank by squeezing fluorine alloy pump.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115926016A (en) * | 2022-12-19 | 2023-04-07 | 山东洁晶集团股份有限公司 | Method for improving transparency and reducing turbidity of sodium alginate produced by calcification method |
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2013
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115926016A (en) * | 2022-12-19 | 2023-04-07 | 山东洁晶集团股份有限公司 | Method for improving transparency and reducing turbidity of sodium alginate produced by calcification method |
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