CN110904465A - Device and method for treating byproduct mirabilite of viscose factory - Google Patents
Device and method for treating byproduct mirabilite of viscose factory Download PDFInfo
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- CN110904465A CN110904465A CN201911007250.7A CN201911007250A CN110904465A CN 110904465 A CN110904465 A CN 110904465A CN 201911007250 A CN201911007250 A CN 201911007250A CN 110904465 A CN110904465 A CN 110904465A
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Abstract
The invention belongs to the technical field of solid waste treatment processes, and particularly relates to a device and a method for treating byproduct mirabilite of a viscose factory. The device comprises a blending tank, a first delivery pump, a pH adjusting tank, a sedimentation tank, a second delivery pump, a filter, bipolar membrane electrodialysis equipment, a third delivery pump, an alkali chamber storage tank, a salt chamber storage tank, an acid chamber storage tank, a second reflux pump, a third reflux pump, a fourth reflux pump, a sixth delivery pump and a sewage discharge pipeline, wherein the sedimentation tank is arranged below the pH adjusting tank. The method for treating the mirabilite comprises the steps of mixing the mirabilite with soft water in a dissolving tank, and then well removing impurities from the mixed solution through impurity removal operations of a pH adjusting tank, a sedimentation tank and a filter. Then electrolyzing by a bipolar membrane electrodialysis device. And when the conductivity of the filtrate in the salt chamber of the bipolar membrane electrodialysis equipment is less than or equal to 20mS/cm, completing the sodium sulfate treatment of the filtrate in the salt chamber and reaching the discharge standard.
Description
Technical Field
The invention belongs to the technical field of solid waste treatment processes, and particularly relates to a device and a method for treating byproduct mirabilite of a viscose factory.
Background
The mirabilite is sulfate mineral mirabilite familyNatrii sulfas, mainly containing aqueous sodium sulfate (Na)2SO4·10H2O). In viscose production, a large amount of mirabilite is additionally generated. The production process is that the viscose solution is sprayed from a spinneret to contact with a coagulating bath, so that the viscose solution and sulfuric acid in the coagulating bath are subjected to chemical reaction to generate sodium sulfate. As production proceeds, the sulfuric acid content in the coagulation bath decreases and the sodium sulfate content increases. Therefore, the coagulation bath needs to precipitate the excess sodium sulfate as a cold crystal before returning to the spinning machine. The separated sodium sulfate is mirabilite. The bipolar membrane electrodialysis device comprises a cathode chamber, an acid chamber, a salt chamber, an alkali chamber and an anode chamber which are sequentially connected in series. The cathode chamber and the acid chamber are connected in series through a bipolar membrane, the acid chamber and the salt chamber are connected in series through an anode membrane, the salt chamber and the alkali chamber are connected in series through a cathode membrane, and the alkali chamber and the anode chamber are connected in series through a bipolar membrane.
The existing method for treating mirabilite is to remove crystal water of mirabilite and then change the crystal water into anhydrous sodium sulphate for sale. Due to the influence of the reduction of market demand, a large amount of anhydrous sodium sulphate can not be treated when being stacked in a viscose factory, thereby bringing great pressure to environmental protection and sale.
Therefore, an apparatus and a method for effectively treating a large amount of mirabilite which is a by-product of a viscose factory are lacked.
Disclosure of Invention
One of the objectives of the present invention is to provide a device for treating byproduct mirabilite in a viscose factory, in order to solve the technical problem that the prior art in the background art lacks a device capable of effectively treating a large amount of byproduct mirabilite in the viscose factory.
The technical scheme for solving the technical problems is as follows: the utility model provides a handle device of viscose factory accessory substance glauber's salt, includes allotment jar, first delivery pump, pH adjusting tank, sedimentation tank, second delivery pump, filter, bipolar membrane electrodialysis equipment, third delivery pump, fourth delivery pump, fifth delivery pump, alkali room storage tank, salt room storage tank, acid room storage tank, second backwash pump, third backwash pump, fourth backwash pump, sixth delivery pump and sewage pipes, bipolar membrane electrodialysis equipment includes cathode chamber, alkali room, salt room, acid room and anode chamber, wherein:
the outlet of the blending tank is communicated with the inlet of the pH adjusting tank through the first delivery pump;
an outlet of the pH adjusting tank is communicated with an inlet of the sedimentation tank through a pipeline, and an outlet of the sedimentation tank is communicated with an inlet of the filter through the second conveying pump;
the outlet of the filter is communicated with the salt chamber storage tank through the third delivery pump;
the salt chamber storage tank is communicated with an inlet of the salt chamber through a third reflux pump, the acid chamber storage tank is communicated with an inlet of the acid chamber through a fourth reflux pump, and the alkali chamber storage tank is communicated with an inlet of the alkali chamber through a second reflux pump;
outlets of the alkali chamber, the salt chamber and the acid chamber are respectively communicated with an alkali chamber storage tank, a salt chamber storage tank and an acid chamber storage tank through pipelines;
the output end of the fourth delivery pump is communicated with the acid chamber storage tank through a pipeline; the output end of the fifth delivery pump is communicated with the alkali chamber storage tank through a pipeline, and the outlet of the salt chamber storage tank is communicated with a sewage pipeline through a sixth delivery pump.
The invention has the beneficial effects that: the solid mirabilite is mixed with soft water in a blending tank to form a mirabilite mixed solution, which contains a large amount of sodium sulfate. And then, the pH value of the pH adjusting tank can be adjusted by sodium hydroxide through adjustment in the pH adjusting tank, and the sodium hydroxide is combined with zinc ions in the mirabilite to generate zinc hydroxide precipitate, so that the zinc ions are removed, and the interference is well avoided. The sedimentation of sedimentation tank makes impurity such as silt of mixed solution precipitate to the bottom, has purified mixed solution, and the filter through setting is further filtered mixed solution's insoluble impurity, fine the interference of avoiding impurity in the mixed solution, more is favorable to the processing of mirabilite. And starting electrolysis of the bipolar membrane electrodialysis device. Water is decomposed on two bipolar membranes, hydroxide radicals enter an alkali chamber, hydrogen ions enter an acid chamber, sodium ions in a salt chamber enter the alkali chamber through a cationic membrane under the action of a direct current power supply, and sodium hydroxide is formed in the alkali chamber; the sulfate ions pass through the anion membrane into the acid chamber where sulfuric acid is formed. Thereby decomposing the sodium sulfate in the filtrate in the salt chamber, realizing the environment-friendly treatment of the mirabilite and not introducing other harmful substances. Due to the arrangement of the second reflux pump, the third reflux pump and the fourth reflux pump, the solution in the bipolar membrane electrodialysis equipment can circulate among the alkali chamber storage tank, the salt chamber storage tank and the acid chamber storage tank, so that the stable conductivity in the bipolar membrane electrodialysis equipment is kept. Due to the arrangement of the sewage discharge pipeline and the sixth delivery pump, filtrate in the salt room in the bipolar membrane electrodialysis equipment, which is electrolyzed to meet the discharge standard, is continuously discharged through the sixth delivery pump and the sewage discharge pipeline. Fresh filtrate continuously flows into a salt chamber of the bipolar membrane electrodialysis device to replenish the solution after reaction. The device provided by the invention can solve the technical problem that a device capable of effectively treating a large amount of byproduct mirabilite of a viscose factory is lacked in the prior art, and provides the device for treating the byproduct mirabilite of the viscose factory. The bipolar membrane electrodialysis device can adopt CJBMED-2040 type bipolar membrane electrodialysis device produced by Sophiaceae high polymer material science and technology limited.
On the basis of the technical scheme, the invention can be further improved as follows.
Further, still include utmost point room storage tank, first reflux pump, first vapour and liquid separator, second vapour and liquid separator and collection pump, wherein:
an outlet of the polar chamber storage tank is communicated with an inlet of the cathode chamber through the first backflow pump, and an output end of the first backflow pump is respectively communicated with the cathode chamber and the anode chamber through pipelines;
the top wall of the cathode chamber and the top wall of the anode chamber are respectively communicated with inlets of the first gas-liquid separator and the second gas-liquid separator through pipelines;
the liquid outlets of the first gas-liquid separator and the second gas-liquid separator are communicated with the input end of the collecting pump through pipelines, and the output end of the collecting pump is communicated with the inlet of the polar chamber storage tank through a pipeline.
The adoption of the further scheme has the beneficial effects that both the first gas-liquid separator and the second gas-liquid separator can adopt the model dn of the Yanuno brand manufactured by Handan Yanuno valve pipe fitting manufacturing company Limited. Since the acid chamber in the bipolar membrane electrodialysis device generates hydrogen and the alkali chamber generates oxygen during electrolysis, the hydrogen and the oxygen respectively enter the first gas-liquid separator and the second gas-liquid separator through two pipelines communicated through the top wall during the ascending process. The liquid separated by the first gas-liquid separator and the second gas-liquid separator returns to the polar chamber storage tank through the collecting pump, and the polar chamber storage tank can effectively return the separated liquid to the cathode chamber and the anode chamber of the bipolar membrane electrodialysis device again for electrolysis, so that the cyclic utilization of energy is realized.
Further, still include first drying tower, second drying tower, third drying tower, fourth drying tower, hydrogen storage tank and oxygen storage tank, wherein:
a gas outlet of the first gas-liquid separator is respectively communicated with inlets of the first drying tower and the second drying tower through pipelines, and a gas outlet of the second gas-liquid separator is respectively communicated with inlets of the third drying tower and the fourth drying tower through pipelines;
outlets of the first drying tower and the second drying tower are communicated with the hydrogen storage tank through pipelines, and outlets of the third drying tower and the fourth drying tower are communicated with the oxygen storage tank through pipelines.
The beneficial effect of adopting above-mentioned further scheme is that, the gas through first vapour and liquid separator and second vapour and liquid separator still has a small amount of liquid, through the alternate work of first drying tower and second drying, and when first drying tower work, the second drying tower overhauls and the change of drier. And a better drying effect is kept. So, dry hydrogen and oxygen can be obtained in the hydrogen storage tank and the oxygen storage tank in the same way.
Furthermore, the input end of the fourth delivery pump, the input end of the fifth delivery pump, the outlet of the acid chamber storage tank and the outlet of the alkali chamber storage tank are all externally connected with pipelines.
The method has the advantages that in the electrolysis process, one part of liquid in the storage tank of the acid chamber flows out as the product dilute sulfuric acid, the other part of liquid returns to the acid chamber of the bipolar membrane electrodialysis equipment by the fourth reflux pump to be continuously electrolyzed, and meanwhile, fresh soft water is supplemented by the fourth delivery pump to reduce the concentration of acid; and one part of the liquid in the storage tank of the alkali chamber flows out as the product sodium hydroxide, and the other part of the liquid is returned to the alkali chamber of the bipolar membrane electrodialysis equipment by using a second reflux pump to continue electrolysis, and meanwhile, fresh soft water is continuously added through a fifth delivery pump to reduce the concentration of the alkali.
Further, the outer walls of the alkali chamber storage tank, the salt chamber storage tank and the acid chamber storage tank are all provided with heat exchange pipelines.
The beneficial effect of adopting above-mentioned further scheme is that, owing to set up the heat transfer pipeline, so electrolyte that because the electrolysis and heaied up can reduce below 25 ℃, the heat transfer pipeline coils on the outer wall of alkali chamber storage tank, salt room storage tank and sour room storage tank, and the entry and the export of heat transfer pipeline set up respectively in the top and the bottom of the outer wall of alkali chamber storage tank, salt room storage tank and sour room storage tank.
The second objective of the present invention is to provide a method for treating mirabilite by using the above device for treating byproduct mirabilite of viscose factory, and the technical solution of the present invention to solve the above technical problems is as follows:
a method of treating glauber's salt comprising the steps of:
A. mirabilite and soft water are mixed according to the mass ratio of 1: (3.4-7.8), respectively adding the mixture into a blending tank from an inlet of the blending tank to obtain a mixed solution; then conveying the mixed solution into a pH adjusting tank by a first conveying pump, and adjusting the pH value of the mixed solution to 8-11; then, allowing the mixed solution in the pH adjusting tank to enter a sedimentation tank, and standing for 2-4 hours;
B. b, conveying the supernatant in the sedimentation tank in the step A to a filter by a second conveying pump for filtering, conveying the obtained filtrate to a storage tank of a salt room by a third conveying pump, and circularly flowing the filtrate between the storage tank of the salt room and the salt room by a third reflux pump;
C. respectively adding soft water with the same volume as the filtrate in the step B into an acid chamber storage tank and an alkali chamber storage tank, then circularly flowing the soft water between the acid chamber storage tank and the acid chamber through a second reflux pump, circularly flowing the soft water between the alkali chamber storage tank and the alkali chamber through a fourth reflux pump, then electrolyzing the bipolar membrane electrodialysis equipment under the conditions that the voltage is 35-45V and the current is 25-35A, and discharging the filtrate through a sewage discharge pipeline through a sixth conveying pump when the conductivity of the filtrate in the salt chamber is less than or equal to 20 mS/cm.
The invention has the beneficial effects that: through the electrolysis in the steps, mirabilite can be effectively electrolyzed, so that sodium sulfate in the mirabilite is decomposed, and the filtrate reaches the discharge standard. Due to the arrangement of the second reflux pump, the third reflux pump and the fourth reflux pump, the solution in the bipolar membrane electrodialysis equipment can circulate among the alkali chamber storage tank, the salt chamber storage tank and the acid chamber storage tank, and the stirring effect is achieved. Thereby keeping stable conductivity in the bipolar membrane electrodialysis device. Therefore, the electrolysis of the filtrate is more thorough, and the treatment method of the mirabilite does not introduce other impurities, has small pollution, and is highly efficient and environment-friendly. And the invention keeps continuous electrolysis, which can make the above process more continuous and efficient.
On the basis of the technical scheme, the invention can be further improved as follows.
Further, in the step A, the temperature of the soft water is 30-55 ℃; pure sodium hydroxide solid is adopted for adjusting the pH value of the mixed solution;
in the step B, the filter 5 adopts a filter screen of 80-160 meshes for filtering.
Adopt the beneficial effect of above-mentioned further scheme to be, the soft water of above-mentioned temperature makes the better solution that dissolves of fixed mirabilite obtain mixed solution. The mixing effect can also be enhanced by stirring in a blending tank, wherein the stirring speed is 50-100r/min, and the stirring time is 1-2 hours. The above filter can filter out impurities which cannot be precipitated well.
Further, in the step C, when the bipolar membrane electrodialysis device carries out electrolysis, the first gas-liquid separator and the second gas-liquid separator collect gas overflowing from the cathode chamber and the anode chamber respectively;
the liquid separated by the first gas-liquid separator and the second gas-liquid separator is conveyed into a polar chamber storage tank through a collecting pump, and the liquid in the polar chamber storage tank is conveyed into the cathode chamber and the anode chamber respectively by a first backflow pump;
and the gas separated by the first gas-liquid separator and the second gas-liquid separator enters a hydrogen storage tank and an oxygen storage tank respectively.
The beneficial effect of adopting the further scheme is that the hydrogen and the oxygen from the bipolar membrane electrodialysis equipment can be well collected through the hydrogen storage tank and the oxygen storage tank. Realizes the reutilization of waste and improves the value of the method.
Further, the gas separated by the first gas-liquid separator is dried by a first drying tower or a second drying tower and then enters the hydrogen storage tank, and the gas separated by the second gas-liquid separator enters the oxygen storage tank after passing through a third drying tower or a fourth drying tower.
The beneficial effect of adopting above-mentioned further scheme is that, the moisture content of the hydrogen and the oxygen of gathering like this is little, and the quality is high.
Further, in step C, when the pH of the solution in the alkaline chamber storage tank is 14, the solution in the alkaline chamber storage tank is taken out;
and when the pH value of the solution in the acid chamber storage tank is 0, taking out the solution in the acid chamber storage tank.
The further scheme has the beneficial effects that under the action of the direct current power supply, sodium ions in the salt chamber enter the alkali chamber through the cationic membrane to form sodium hydroxide in the alkali chamber; the sulfate ions pass through the anion membrane into the acid chamber where sulfuric acid is formed. Therefore, the alkali chamber storage tank and the acid chamber storage tank realize the collection of sulfuric acid and sodium hydroxide and realize the waste utilization.
Drawings
FIG. 1 is a schematic flow diagram of an apparatus for treating byproduct mirabilite in a viscose factory according to the present invention;
in the drawings, the components represented by the respective reference numerals are listed below:
1. a blending tank, 2, a first delivery pump, 3, a pH adjusting tank, 4, a sedimentation tank, 5, a filter, 601, a polar chamber storage tank, 602, an alkali chamber storage tank, 603, a salt chamber storage tank, 604, an acid chamber storage tank, 701, a first reflux pump, 702, a second reflux pump, 703, a third reflux pump, 704, a fourth reflux pump, 8, a gas-liquid separator, 801, a first gas-liquid separator, 802, a second gas-liquid separator, 9, a drying tower, 901, a first drying tower, 902, a second drying tower, 903, a third drying tower, 904, a fourth drying tower, 1001, hydrogen storage tank, 1002, an oxygen storage tank, 11, a second delivery pump, 12, a third delivery pump, 13, a collecting pump, 14, a fourth delivery pump, 15, a fifth delivery pump, 16, a bipolar membrane electrodialysis device, 1601, cathode chamber, 1602, an alkali chamber, 1603, a salt chamber, 1604, an acid chamber, 1605, an anode chamber, 17, a sewage discharge pipeline, 18, a salt chamber, and a sixth delivery pump.
Detailed Description
The principles and features of this invention are described below in conjunction with the following drawings, which are set forth by way of illustration only and are not intended to limit the scope of the invention.
As shown in fig. 1, an apparatus for treating mirabilite, a byproduct of a viscose factory, comprises a blending tank 1, a first delivery pump 2, a pH adjusting tank 3, a sedimentation tank 4, a second delivery pump 11, a filter 5, a bipolar membrane electrodialysis device 16, a third delivery pump 12, a fourth delivery pump 14, a fifth delivery pump 15, an alkali chamber storage tank 602, a salt chamber storage tank 603, an acid chamber storage tank 604, a second reflux pump 702, a third reflux pump 703, a fourth reflux pump 704, a sixth delivery pump 18 and a sewage discharge pipeline 17, wherein: the outlet of the blending tank 1 is communicated with the inlet of the pH adjusting tank 3 through the first delivery pump 2; the outlet of the pH adjusting tank 3 is communicated with the inlet of the sedimentation tank 4 through a pipeline, and the outlet of the sedimentation tank 4 is communicated with the inlet of the filter 5 through the second conveying pump 11; the outlet of the filter 5 is communicated with the salt room storage tank 603 through the third delivery pump 12; the bipolar membrane electrodialysis device 16 comprises a cathode chamber 1601, an alkali chamber 1602, a salt chamber 1603, an acid chamber 1604 and an anode chamber 1605, the salt chamber storage tank 603 is communicated with an inlet of the salt chamber 1603 through the third reflux pump 703, the acid chamber storage tank 604 is communicated with an inlet of the acid chamber 1604 through the fourth reflux pump 704, and the alkali chamber storage tank 602 is communicated with an inlet of the alkali chamber 1602 through the second reflux pump 702; the outlets of the alkali chamber 1602, the salt chamber 1603 and the acid chamber 1604 are respectively communicated with the alkali chamber storage tank 602, the salt chamber storage tank 603 and the acid chamber storage tank 604 through pipelines; the output end of the fourth delivery pump 14 is communicated with the acid chamber storage tank 604 through a pipeline; the output end of the fifth delivery pump 15 is communicated with the alkali chamber storage tank 602 through a pipeline, and the outlet of the salt chamber storage tank 603 is communicated with the sewage pipeline 17 through the sixth delivery pump 18. Gate valves are arranged on a pipeline between the blending tank 1 and the pH adjusting tank 3, a pipeline between the pH adjusting tank 3 and the sedimentation tank 4, a pipeline between the sedimentation tank 4 and the filter 5, the salt chamber storage tank 603 and the sewage discharge pipeline 17.
Optionally, the system further comprises a polar chamber storage tank 601, a first reflux pump 701, a gas-liquid separator 8 and a collecting pump 13, wherein the gas-liquid separator 8 comprises a first gas-liquid separator 801 and a second gas-liquid separator 802 which are arranged in parallel, an outlet of the polar chamber storage tank 601 is communicated with the cathode chamber 1601 through the first reflux pump 701, and an output end of the first reflux pump 701 is communicated with the cathode chamber 1601 and the anode chamber 1605 through pipelines respectively; the top wall of the cathode chamber 1601 and the top wall of the anode chamber 1605 are respectively communicated with inlets of the first gas-liquid separator 801 and the second gas-liquid separator 802 through pipes; the liquid outlets of the first gas-liquid separator 801 and the second gas-liquid separator 802 are both communicated with the input end of the collecting pump 13 through a pipeline, and the output end of the collecting pump 13 is communicated with the inlet of the polar chamber storage tank 601 through a pipeline.
Optionally, the drying system further comprises a drying tower 9, a hydrogen storage tank 1001 and an oxygen storage tank 1002, wherein the drying tower 9 comprises a first drying tower 901, a second drying tower 902, a third drying tower 903 and a fourth drying tower 904 which are arranged in parallel, a gas outlet of the first gas-liquid separator 801 is communicated with inlets of the first drying tower 901 and the second drying tower 902 through a pipeline, respectively, and a gas outlet of the second gas-liquid separator 802 is communicated with inlets of the third drying tower 903 and the fourth drying tower 904 through a pipeline, respectively; the outlets of the first drying tower 901 and the second drying tower 902 are both communicated with the hydrogen storage tank 1001 through pipelines, and the outlets of the third drying tower 903 and the fourth drying tower 904 are both communicated with the oxygen storage tank 1002 through pipelines.
Optionally, an input end of the fourth delivery pump 14, an input end of the fifth delivery pump 15, an outlet of the acid chamber storage tank 604, and an outlet of the alkali chamber storage tank 602 are all externally connected with a pipeline.
Optionally, the outer walls of the alkali chamber storage tank 602, the salt chamber storage tank 603, and the acid chamber storage tank 604 are all provided with heat exchange pipes. A pH meter is provided in each of the cathode chamber 1601, the alkali chamber 1602, the salt chamber 1603, the acid chamber 1604, and the anode chamber 1605. And a conductivity meter is also arranged in the salt chamber 1603.
In a specific mirabilite treatment process, the method for treating the mirabilite by using the device for treating the byproduct mirabilite of the viscose factory comprises the following steps:
A. mirabilite and soft water are mixed according to the mass ratio of 1: (3.4-7.8), respectively adding the mixture into the blending tank 1 from the inlet of the blending tank 1 to obtain a mixed solution; then, the mixed solution is conveyed into a pH adjusting tank 3 by a first conveying pump 2, the pH value of the mixed solution is adjusted to 8-11, and then the mixed solution enters a sedimentation tank 4 and stands for 2-4 hours;
B. the second delivery pump 11 delivers the supernatant in the sedimentation tank 4 in the step a to the filter 5 for filtration, the obtained filtrate is delivered to the salt room storage tank 603 through the third delivery pump 12, and the filtrate circularly flows between the salt room storage tank 603 and the salt room 1603 through the third reflux pump 703;
C. adding soft water with the same volume as the filtrate in the step B into an acid chamber storage tank 604 and a base chamber storage tank 602 respectively, then circularly flowing the soft water between the acid chamber storage tank 604 and the acid chamber 1604 through a second reflux pump 702, circularly flowing the soft water between the base chamber storage tank 603 and a base chamber 1602 through a fourth reflux pump 704, then electrolyzing the bipolar membrane electrodialysis device 16 under the conditions that the voltage is 35-45V and the current is 25-35A, and when the conductivity of the filtrate in the salt chamber 1603 is less than or equal to 20mS/cm, discharging the filtrate through a sewage discharge pipeline 17 through a sixth conveying pump 18.
Optionally, in the step A, the temperature of the soft water is 30-55 ℃; pure sodium hydroxide solid is adopted for adjusting the pH value of the mixed solution; in the step B, the filter 5 adopts a filter screen of 80-160 meshes for filtering.
Optionally, in step C, when the bipolar membrane electrodialysis device 16 performs electrolysis, the first gas-liquid separator 801 and the second gas-liquid separator 802 collect gas overflowing from the cathode chamber 1601 and the anode chamber 1605, respectively; the liquid separated by the first gas-liquid separator 801 and the second gas-liquid separator 802 is delivered to the polar chamber storage tank 601 by the collecting pump 13, and the first backflow pump 701 further delivers the liquid in the polar chamber storage tank 601 to the cathode chamber 1601 and the anode chamber 1605, respectively; the gas separated by the first gas-liquid separator 801 and the second gas-liquid separator 802 enters a hydrogen storage tank 1001 and an oxygen storage tank 1002, respectively.
Optionally, the gas separated by the first gas-liquid separator 801 is dried by the first drying tower 901 or the second drying tower 902 and then enters the hydrogen storage tank 1001, and the gas separated by the second gas-liquid separator 802 enters the oxygen storage tank 1002 after passing through the third drying tower 903 or the fourth drying tower 904.
Optionally, in step C, when the pH of the solution in the alkali chamber storage tank 602 is 14, taking out the solution in the alkali chamber storage tank 602; when the pH of the solution in the acid chamber storage tank 604 is 0, the solution in the acid chamber storage tank 604 is taken out.
Examples 2,
The difference from example 1 is that during the specific mirabilite treatment process, mirabilite and soft water were mixed in a ratio of 1: 5 is added into the dissolving tank 1 to obtain a mixed solution.
Examples 3,
In a specific mirabilite treatment process, in step a, mirabilite and soft water are mixed according to a ratio of 1: 7.8 to obtain a mixed solution.
In the present invention, the term "plurality" means two or more unless explicitly defined otherwise. The terms "mounted," "connected," "fixed," and the like are to be construed broadly, and for example, "connected" may be a fixed connection, a removable connection, or an integral connection; "coupled" may be direct or indirect through an intermediary. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", and the like indicate orientations or positional relationships based on those shown in the drawings, and are merely for convenience of description and simplicity of description, and do not indicate or imply that the referred device or unit must have a specific direction, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
In the description herein, the description of the terms "one embodiment," "some embodiments," "specific embodiments," etc., means that a particular feature, structure, material, or characteristic described in connection with the embodiment or example is included in at least one embodiment or example of the invention. In this specification, the schematic representations of the terms used above do not necessarily refer to the same embodiment or example. Furthermore, the particular features, structures, materials, or characteristics described may be combined in any suitable manner in any one or more embodiments or examples.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. The device for treating the byproduct mirabilite in the viscose factory is characterized by comprising a preparation tank (1), a first delivery pump (2), a pH adjusting tank (3), a sedimentation tank (4), a second delivery pump (11), a filter (5), bipolar membrane electrodialysis equipment (16), a third delivery pump (12), a fourth delivery pump (14), a fifth delivery pump (15), an alkali chamber storage tank (602), a salt chamber storage tank (603), an acid chamber storage tank (604), a second reflux pump (702), a third reflux pump (703), a fourth reflux pump (704), a sixth delivery pump (18) and a sewage discharge pipeline (17);
the outlet of the blending tank (1) is communicated with the inlet of the pH adjusting tank (3) through the first delivery pump (2);
the outlet of the pH adjusting tank (3) is communicated with the inlet of the sedimentation tank (4) through a pipeline, and the outlet of the sedimentation tank (4) is communicated with the inlet of the filter (5) through the second conveying pump (11);
the outlet of the filter (5) is communicated with the salt room storage tank (603) through the third delivery pump (12);
the bipolar membrane electrodialysis device (16) comprises a cathode chamber (1601), an alkali chamber (1602), a salt chamber (1603), an acid chamber (1604) and an anode chamber (1605), wherein the salt chamber storage tank (603) is communicated with an inlet of the salt chamber (1603) through the third reflux pump (703), the acid chamber storage tank (604) is communicated with an inlet of the acid chamber (1604) through the fourth reflux pump (704), and the alkali chamber storage tank (602) is communicated with an inlet of the alkali chamber (1602) through the second reflux pump (702);
outlets of the alkali chamber (1602), the salt chamber (1603) and the acid chamber (1604) are respectively communicated with the alkali chamber storage tank (602), the salt chamber storage tank (603) and the acid chamber storage tank (604) through pipelines;
the output end of the fourth delivery pump (14) is communicated with the acid chamber storage tank (604) through a pipeline; the output end of the fifth delivery pump (15) is communicated with the alkali chamber storage tank (602) through a pipeline, and the outlet of the salt chamber storage tank (603) is communicated with the sewage discharge pipeline (17) through the sixth delivery pump (18).
2. The apparatus for treating the mirabilite as the byproduct of the viscose factory according to claim 1, further comprising a polar room storage tank (601), a first reflux pump (701), a gas-liquid separator (8) and a collection pump (13), wherein the gas-liquid separator (8) comprises a first gas-liquid separator (801) and a second gas-liquid separator (802) which are arranged in parallel, and wherein:
an outlet of the polar chamber storage tank (601) is communicated with an inlet of the cathode chamber (1601) through the first backflow pump (701), and an output end of the first backflow pump (701) is communicated with the cathode chamber (1601) and the anode chamber (1605) through pipelines respectively;
the top wall of the cathode chamber (1601) and the top wall of the anode chamber (1605) are respectively communicated with inlets of the first gas-liquid separator (801) and the second gas-liquid separator (802) through pipelines;
liquid outlets of the first gas-liquid separator (801) and the second gas-liquid separator (802) are communicated with an input end of the collecting pump (13) through pipelines, and an output end of the collecting pump (13) is communicated with an inlet of the polar chamber storage tank (601) through a pipeline.
3. The apparatus for treating the mirabilite as a byproduct of the viscose factory according to claim 2, further comprising a drying tower (9), a hydrogen storage tank (1001) and an oxygen storage tank (1002), wherein the drying tower (9) comprises a first drying tower (901), a second drying tower (902), a third drying tower (903) and a fourth drying tower (904) which are arranged in parallel, wherein:
the gas outlet of the first gas-liquid separator (801) is communicated with the inlets of the first drying tower (901) and the second drying tower (902) through pipelines respectively, and the gas outlet of the second gas-liquid separator (802) is communicated with the inlets of the third drying tower (903) and the fourth drying tower (904) through pipelines respectively;
the outlets of the first drying tower (901) and the second drying tower (902) are communicated with the hydrogen storage tank (1001) through pipelines, and the outlets of the third drying tower (903) and the fourth drying tower (904) are communicated with the oxygen storage tank (1002) through pipelines.
4. The apparatus for treating byproduct mirabilite in viscose factory according to claim 1, characterized in that the input of the fourth transfer pump (14), the input of the fifth transfer pump (15), the outlet of the acid chamber storage tank (604) and the outlet of the alkali chamber storage tank (602) are all externally connected with pipelines.
5. The apparatus for treating byproduct mirabilite in viscose factory according to claim 1, wherein the outer walls of the alkali chamber storage tank (602), the salt chamber storage tank (603) and the acid chamber storage tank (604) are all provided with heat exchange pipes.
6. The method for treating the mirabilite by using the device for treating the byproduct mirabilite of the viscose factory according to any one of claims 1 to 5 is characterized by comprising the following steps:
A. mirabilite and soft water are mixed according to the mass ratio of 1: (3.4-7.8), respectively adding the mixture into the blending tank (1) from an inlet of the blending tank (1) to obtain a mixed solution; then conveying the mixed solution into a pH adjusting tank (3) by a first conveying pump (2), adjusting the pH value of the mixed solution to 8-11, then feeding the mixed solution into the sedimentation tank (4), and standing for 2-4 hours;
B. conveying the supernatant in the sedimentation tank (4) in the step A to a filter (5) by a second conveying pump (11) for filtering, conveying the obtained filtrate to a salt chamber storage tank (603) by a third conveying pump (12), and circulating the filtrate between the salt chamber storage tank (603) and a salt chamber (1603) by a third reflux pump (703);
C. respectively adding soft water with the same volume as the filtrate in the step B into an acid chamber storage tank (604) and a base chamber storage tank (602), then circularly flowing the soft water between the acid chamber storage tank (604) and the acid chamber (1604) through a second reflux pump (702), circularly flowing the soft water between the base chamber storage tank (603) and a base chamber (1602) through a fourth reflux pump (704), then electrolyzing the bipolar membrane electrodialysis device (16) under the conditions that the voltage is 35-45V and the current is 25-35A, and discharging the filtrate through a blowdown pipeline (17) through a sixth conveying pump (18) when the conductivity of the filtrate in the salt chamber (1603) is less than or equal to 20 mS/cm.
7. The method for treating mirabilite according to claim 6, wherein in step A, the temperature of the soft water is 30-55 ℃; pure sodium hydroxide solid is adopted for adjusting the pH value of the mixed solution;
in the step B, the filter (5) adopts a filter screen of 80-160 meshes for filtering.
8. The method for treating mirabilite according to claim 6, characterized in that in step C, when the bipolar membrane electrodialysis device (16) performs electrolysis, the first gas-liquid separator (801) and the second gas-liquid separator (802) collect the gas overflowing from the cathode chamber (1601) and the anode chamber (1605), respectively;
the liquid separated by the first gas-liquid separator (801) and the second gas-liquid separator (802) is conveyed into a polar chamber storage tank (601) through a collecting pump (13), and then the liquid in the polar chamber storage tank (601) is conveyed into the cathode chamber (1601) and the anode chamber (1605) respectively by a first backflow pump (701);
the gases separated by the first gas-liquid separator (801) and the second gas-liquid separator (802) enter a hydrogen storage tank (1001) and an oxygen storage tank (1002) respectively.
9. The method for processing mirabilite according to claim 8, characterized in that the gas separated by the first gas-liquid separator (801) is dried by a first drying tower (901) or a second drying tower (902) and then enters the hydrogen storage tank (1001), and the gas separated by the second gas-liquid separator (802) enters the oxygen storage tank (1002) after passing through a third drying tower (903) or a fourth drying tower (904).
10. The method of processing mirabilite of claim 6, wherein in step C, when the pH of the solution in the base chamber reservoir (602) is 14, the solution in the base chamber reservoir (602) is removed;
when the pH value of the solution in the acid chamber storage tank (604) is 0, the solution in the acid chamber storage tank (604) is taken out.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112939295A (en) * | 2021-03-25 | 2021-06-11 | 四川恩特普环保科技有限公司 | Method for preparing acid and alkali by sodium sulfate bipolar membrane electrodialysis |
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Effective date of registration: 20200812 Address after: 843300 East 755 Wei2 Road, No. 2 Industrial Park, Alar City, Xinjiang Uygur Autonomous Region Applicant after: Alar Zhongtai Textile Technology Co.,Ltd. Applicant after: XINJIANG ZHONGTAI INNOVATION TECHNOLOGY RESEARCH INSTITUTE Co.,Ltd. Address before: Room 509, 5th floor, 39 Yangchenghu Road, Urumqi Economic and Technological Development Zone, Xinjiang Uygur Autonomous Region Applicant before: XINJIANG ZHONGTAI INNOVATION TECHNOLOGY RESEARCH INSTITUTE Co.,Ltd. |
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