CN111333086B - Preparation method and device for realizing new technology of total-halogen alkali preparation - Google Patents
Preparation method and device for realizing new technology of total-halogen alkali preparation Download PDFInfo
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- CN111333086B CN111333086B CN202010162886.5A CN202010162886A CN111333086B CN 111333086 B CN111333086 B CN 111333086B CN 202010162886 A CN202010162886 A CN 202010162886A CN 111333086 B CN111333086 B CN 111333086B
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- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
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- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
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Abstract
The invention discloses a preparation method and a device for realizing a new technology of full-brine alkali preparation, wherein a polymeric flocculant is added into raw brine, the raw brine is filtered, and brine after separation and precipitation is separated to obtain a nitrate-poor solution and a nitrate-rich solution; evaporating and concentrating the lean nitrate solution, and centrifugally dehydrating and separating to obtain crystal salt; evaporating and concentrating the nitrate-rich solution, and centrifugally dewatering and separating to obtain anhydrous sodium sulphate; returning the salt centrifugation mother liquor and the nitrate-poor residue to perform secondary separation treatment; and mixing the nitrate centrifugal mother liquor and the nitrate-rich residues with the original brine, and then carrying out secondary separation treatment. By removing metal ions such as calcium, magnesium and the like, the influence on evaporation equipment caused by metal ion scaling in brine can be removed; the polymeric flocculant is added, so that flocculate can be removed, and the subsequent influence on the nanofiltration membrane concentration and separation device is reduced; by separately, independently and synchronously evaporating and concentrating the salt and the nitre, the high-quality salt and the anhydrous nitre can be more easily controlled and produced, and the dry-basis quality of the anhydrous sodium sulphate can be improved to 99%.
Description
Technical Field
The invention relates to the technical field of alkali preparation from brine, in particular to a preparation method and a device for realizing a novel full-brine alkali preparation technology.
Background
The raw material brine of the well and mineral salt industry in China is rich, and with the popularization of the mechanical steam recompression fresh brine concentration and crystallization technology, more and more factories with brine resources adopt the mechanical steam recompression technology to evaporate and crystallize brine, so that the production of total brine alkali is realized, the raw material cost is greatly reduced, and the energy consumption is reduced.
At present, the chlor-alkali industry adopts a process of mechanically recompressing full brine for alkali production by vapor, and two common processes are adopted, wherein one process is a process combining membrane method freezing denitration and light brine concentration, namely, firstly membrane method freezing denitration is adopted to obtain a poor nitrate solution andand (3) sodium sulfate decahydrate (mirabilite), wherein the poor nitrate solution is sent to a first-effect mechanical vapor recompression evaporation system for evaporation and concentration, and meanwhile, the sodium sulfate decahydrate (mirabilite) is sent to a second-effect mechanical vapor recompression evaporation system for evaporation, concentration and crystallization after being redissolved by high-temperature condensate water generated by the evaporation system to obtain anhydrous sodium sulfate (anhydrous sodium sulfate). The freezing crystallization of the process is generally to mix nitrate-rich liquid (Na) 2 SO 4 Cooling to-5 deg.C (Na) with a content of 70-100 g/l 2 SO 4 The content is 15-25 g/l), the nitrate precipitation efficiency is high, but refrigeration is needed to consume large energy consumption, sodium sulfate crystallization at low temperature produces sodium sulfate decahydrate (mirabilite) with crystal water, the value is not high, the sodium sulfate crystallization is often needed to be treated as solid waste, and the environmental protection pressure is also large. Further evaporation is required to eliminate the environmental pressure. The sodium sulfate decahydrate (mirabilite) needs additional water to be dissolved, so that the additional evaporation capacity of the system is increased, and the waste of energy is caused.
The process for coproducing salt and sodium sulfate adopts mechanical steam recompression method, and adopts NaCl and Na 2 SO 4 The characteristic of intersolubility relationship at different temperatures adopts a circulating process of high-temperature saltpeter separation, low-temperature saltpeter separation and mother liquor recycling to high-temperature saltpeter separation respectively to produce high-purity salt and anhydrous sodium sulfate (anhydrous sodium sulfate) with sales value step by step. The process needs to be circulated back and forth at high temperature and low temperature, a large amount of cooling water is consumed for cooling, and then steam is consumed for heating, so that the waste of energy is caused. In addition, NaCl and Na are used 2 SO 4 The concentration difference of the precipitation temperature at different temperatures is not changed greatly, the nitrate precipitation efficiency is low, the product quality is not easy to control, the dry basis weight of the anhydrous sodium sulphate is generally 86-96%, and the product value is not high.
Disclosure of Invention
The invention aims to solve the technical problem of providing a preparation method and a device for realizing a new full-brine alkali-making technology, which are applied by the applicant in 2012, on the basis of a salt and nitrate co-production process and device by a mirabilite type brine mechanical vapor recompression method, the process is improved, the original high-low temperature cyclic evaporation crystallization process of salt and nitrate is improved to a separated and independent synchronous evaporation concentration crystallization process, so that high-quality anhydrous nitrate (the dry basis quality of anhydrous sodium sulphate can be improved to 99 percent) can be produced, and the method has the characteristics of energy conservation, higher nitrate precipitation efficiency, low equipment investment, low production cost and the like.
The technical problem is solved through the following technical scheme:
on one hand, the invention provides a preparation method of a new technology for preparing alkali by total halogen, which comprises the following steps:
sequentially adding a sodium carbonate saturated solution and a sodium hydroxide saturated solution into raw brine, adjusting the pH to 10-11, wherein the volume ratio of the raw brine to the sodium carbonate saturated solution to the sodium hydroxide saturated solution is 1000: 45-75: 45-75, adding a polymeric flocculant under stirring, wherein the volume ratio of the raw brine to the polymeric flocculant is 1000:0.1-0.3, and after the flocculation and precipitation are finished, filtering to separate the flocculation and precipitation and remove metal ions such as calcium, magnesium and the like; the brine after separation and precipitation passes through a nanofiltration membrane concentration and separation device to obtain less Na 2 SO 4 The poor nitrate solution (Na) 2 SO 4 Content less than or equal to 2g/l), and is rich in Na 2 SO 4 Nitrate-rich liquid (Na) 2 SO 4 The content is 90-100 g/l); the polymeric flocculant comprises polymeric ferric sulfate, polyacrylamide or the combination of the polymeric ferric sulfate and the polyacrylamide;
less Na 2 SO 4 The lean nitrate solution enters a first-effect evaporation concentration system for evaporation concentration, the temperature of evaporation concentration is controlled to be 80-130 ℃, the pressure is 0.04-0.12 MPa, along with continuous concentration of brine, the concentration of sodium chloride reaches a saturated state, salt slurry is separated out, salt slurry and lean nitrate residues are obtained through filtration, and crystal salt and salt centrifugal mother liquor are obtained through centrifugal dehydration and separation of the salt slurry;
rich in Na 2 SO 4 The rich nitrate solution enters a second-effect evaporation concentration system for evaporation concentration, the temperature of evaporation concentration is controlled to be 90-105 ℃, the pressure is 0.05-0.07 MPa, sodium sulfate is in a supersaturated state, nitrate slurry is continuously separated out, the nitrate slurry and rich nitrate residues are obtained by filtration, and anhydrous sodium sulphate and nitrate centrifugal mother liquor are obtained by centrifugal dehydration and separation of the nitrate slurry;
returning the salt centrifugal mother liquor and the poor nitrate residue to a nanofiltration membrane concentration and separation device for secondary separation treatment;
and mixing the nitrate centrifugal mother liquor and the nitrate-rich residues with the original brine, and then carrying out secondary separation treatment.
On the other hand, the invention provides a device for realizing a new technology for preparing alkali from full brine, which comprises a brine reaction tank, a sedimentation tank, a nanofiltration membrane concentration and separation device, an evaporation concentration system and a centrifugal system which are sequentially communicated;
the evaporation concentration system comprises a first-effect evaporation concentration system and a second evaporation concentration system, wherein:
the first-effect evaporation concentration system is connected with a permeate outlet of the nanofiltration membrane concentration and separation device and is used for carrying out evaporation concentration crystallization treatment on permeate; a salt slurry outlet of the first-effect evaporation concentration system is communicated with the first centrifugal system and the first drying device in sequence; a nitrate-poor residue discharge port of the first-effect evaporation concentration system and a salt centrifugation mother liquor discharge port of the first centrifugal system are communicated with an inlet of the nanofiltration membrane concentration and separation device;
the second-effect evaporation concentration system is connected with a concentrated solution outlet of the nanofiltration membrane concentration separation device and is used for carrying out evaporation concentration crystallization treatment on the concentrated solution; a salt slurry outlet of the second-effect evaporation and concentration system is communicated with the second centrifugal system and the second drying device in sequence; a nitrate-rich residue outlet of the second-effect evaporation concentration system and a nitrate centrifugal mother liquor outlet of the second centrifugal system are communicated with an inlet of the brine reaction tank;
the evaporation concentration system comprises an evaporation kettle, and a plurality of evaporated liquid condensation assemblies are communicated with the evaporation kettle;
the evaporated liquid condensing assembly comprises a condensing kettle, the top of the evaporating kettle is communicated with a condensing pipe, the condensing pipe penetrates through the top of the condensing kettle, the condensing pipe is communicated with a plurality of condensing mechanisms, and the condensing mechanisms are positioned in the condensing kettle;
the condensing mechanism comprises a condensing disc communicated with a condensing pipe, a condensing cavity is formed in the condensing disc, the outer side wall of the condensing disc is communicated with a plurality of annular pipelines, a plurality of condensing balls are annularly distributed on the annular pipelines, and the plurality of condensing balls are distributed on the annular pipelines in an upper layer and a lower layer;
the condensing ball is obliquely communicated with the annular pipeline;
the evaporation concentration system of the new technology for preparing the total halogenated soda also comprises a vacuum component matched with the evaporated liquor condensation component, and vacuum is formed in the condensation kettle through the vacuum component.
Further, the evaporation kettle comprises a kettle body, wherein a jacket is arranged on the kettle body, and the jacket is used for introducing hot steam to heat the kettle body.
Furthermore, 6 evaporating liquid condensing assemblies are communicated with the evaporation kettle;
and 6 evaporative liquid condensing assemblies are distributed on the top of the evaporation kettle in an annular array.
Furthermore, the condensing pipe is communicated with two condensing mechanisms which are arranged at intervals up and down.
Further, the lateral wall of condensate tray intercommunication has a plurality of side end pipe, side end pipe intercommunication is on the inside wall of ring conduit.
Furthermore, a plurality of the condensation balls are distributed at the upper end and the lower end of the annular pipeline in an annular array distribution mode;
the condensing ball is communicated with the annular pipeline through a pipeline;
the condensing ball at the upper end of the annular pipeline is obliquely arranged upwards, and the condensing ball at the lower end of the annular pipeline is obliquely arranged downwards.
Further, the vacuum assembly comprises an annular vacuum pipeline which faces downwards and is communicated with the top of the condensation kettle through a side pipeline;
the annular vacuum pipeline is communicated with a vacuum pump;
a plurality of vacuum through holes are formed in the condensation pipe and are located in the condensation kettle.
Further, the condenser pipe is connected with a valve.
Further, the centrifugal system comprises a base, a centrifugal system body is assembled at the top of the base, a protective cover assembly is connected onto the base in a sliding mode, the protective cover assembly comprises a protective cover located right above the centrifugal system body, and an annular protruding piece is fixedly connected to the edge of the bottom of the protective cover;
the annular convex sheet is connected with a plurality of guide rods in a sliding manner, and the guide rods are fixedly connected to the top of the base;
the centrifugal system is characterized in that the protective cover is provided with a driving assembly, the driving assembly drives the protective cover to move up and down, and the centrifugal system body is covered and opened through the up-and-down movement of the protective cover;
be equipped with a plurality of buffer structure on the inside wall of protection casing, through buffer structure buffers the protection casing and covers when closing centrifugal system body on, the vibration of buffering protection casing.
Further, the drive assembly comprises a drive motor disposed above the shield;
the driving motor is connected with a screw rod downwards, and a screw rod barrel in threaded connection with the screw rod is fixedly connected onto the annular convex plate;
the screw is in threaded connection with the screw barrel;
the lower end of the lead screw is positioned below the annular convex piece.
Further, the annular tabs are fitted with drive assemblies at both their front and rear ends.
Furthermore, a support is fixedly connected to the middle of a driving motor in the driving assembly, which is positioned at the front end and the two ends of the annular protruding piece, and the support is fixedly connected to the base.
Further, the bracket comprises a horizontal end fixedly connected between the driving motors;
the horizontal end is vertically connected with a vertical end which is fixedly connected to the front and rear side walls of the base.
Further, buffer structure all includes the elastic bulge, the bellied lower extreme of elasticity is located the bottom in the protection casing, the bellied upper end of elasticity is located the top in the protection casing.
Further, the bottom fixedly connected with a plurality of bracing piece of base, the bottom fixedly connected with supporting seat of bracing piece.
Compared with the prior art, the preparation method and the device for realizing the new technology of total halogen alkali preparation have the following beneficial effects:
the sodium carbonate and the sodium hydroxide are adopted to remove metal ions such as calcium, magnesium and the like, so that the influence on evaporation equipment caused by metal ion scaling in brine can be removed; the polymeric flocculant is added, so that flocculate can be removed, and the subsequent influence on the nanofiltration membrane concentration and separation device is reduced;
by separately, independently and synchronously evaporating and concentrating the salt and the nitre, the high-quality salt and anhydrous nitre can be more easily controlled and output, and the dry-basis quality of the anhydrous sodium sulphate can be improved to 99%;
the condensation area of the solvent steam is increased through the evaporation concentration system, and the solvent steam is particularly distributed to different condensation pipes and then enters the condensation balls with large surface areas for cooling, so that the concentration and cooling efficiency is improved, and the energy consumption is saved;
removing metal ions such as calcium and magnesium, concentrating the rich nitrate solution (Na) by an evaporation concentration system 2 SO 4 The content is 90-100 g/l), the nitrate precipitation efficiency after evaporation is more than or equal to 25g/l, the NaCl content in the nitrate-rich liquid is generally 200g/l, NaCl is easier to control not to crystallize and precipitate, and the method has the characteristics of more energy conservation, higher nitrate precipitation efficiency, low equipment investment, low production cost and the like.
Drawings
FIG. 1 is a schematic view of the overall structure of an evaporative concentration system according to an embodiment of the present invention;
FIG. 2 is a schematic diagram of an evaporative liquid condensing assembly in an embodiment of the present invention;
FIG. 3 is a top view of the embodiment of the present invention shown in FIG. 1;
FIG. 4 is a schematic diagram of the connection relationship between the condensing ball and the annular pipe in the embodiment of the invention;
FIG. 5 is a schematic structural view of a condensing mechanism in an embodiment of the present invention;
FIG. 6 is a device for implementing a new technology for producing alkali from brine in the embodiment of the invention;
FIG. 7 is a schematic view of the overall structure of a centrifugal system according to an embodiment of the present invention;
FIG. 8 is a schematic diagram of the shield of the centrifuge system in an embodiment of the present invention.
Detailed Description
The following examples are given for the detailed implementation and specific operation of the present invention, but the scope of the present invention is not limited to the following examples.
Example 1
A preparation method of a new technology for preparing alkali by total halogen comprises the following steps:
sequentially adding a sodium carbonate saturated solution and a sodium hydroxide saturated solution into raw brine, adjusting the pH to 10-11, wherein the volume ratio of the raw brine to the sodium carbonate saturated solution to the sodium hydroxide saturated solution is 1000: 45-75: 45-75, adding a polymeric flocculant under stirring, wherein the volume ratio of the raw brine to the polymeric flocculant is 1000:0.1-0.3, and after the flocculation and precipitation are finished, filtering to separate the flocculation and precipitation and remove metal ions such as calcium, magnesium and the like; the brine after separation and precipitation passes through a nanofiltration membrane concentration and separation device to obtain less Na 2 SO 4 The poor nitrate solution (Na) 2 SO 4 Content less than or equal to 2g/l), and is rich in Na 2 SO 4 Nitrate-rich liquid (Na) 2 SO 4 The content is 90-100 g/l); the polymeric flocculant comprises polymeric ferric sulfate, polyacrylamide or the combination of the polymeric ferric sulfate and the polyacrylamide;
less Na 2 SO 4 The lean nitrate solution enters a first-effect evaporation concentration system for evaporation concentration, the temperature of evaporation concentration is controlled to be 80-130 ℃, the pressure is 0.04-0.12 MPa, along with continuous concentration of brine, the concentration of sodium chloride reaches a saturated state, salt slurry is separated out, salt slurry and lean nitrate residues are obtained through filtration, and crystal salt and salt centrifugal mother liquor are obtained through centrifugal dehydration and separation of the salt slurry;
rich in Na 2 SO 4 The rich nitrate solution enters a second-effect evaporation concentration system for evaporation concentration, the temperature of evaporation concentration is controlled to be 90-105 ℃, the pressure is 0.05-0.07 MPa, sodium sulfate is in a supersaturated state, nitrate slurry is continuously separated out, the nitrate slurry and rich nitrate residues are obtained by filtration, and anhydrous sodium sulphate and nitrate centrifugal mother liquor are obtained by centrifugal dehydration and separation of the nitrate slurry;
returning the salt centrifugal mother liquor and the poor nitrate residue to a nanofiltration membrane concentration and separation device for secondary separation treatment;
and mixing the nitrate centrifugal mother liquor and the nitrate-rich residues with the original brine, and then carrying out secondary separation treatment.
By applying the preparation method of the invention, Na in the obtained nitrate-rich liquid 2 SO 4 The content of the sodium sulfate is 90-100 g/l, the nitrate separating efficiency after evaporation is more than or equal to 25g/l, the NaCl content in the nitrate-rich liquid is generally 200g/l, the NaCl is easier to control not to crystallize and separate out, and high-quality anhydrous sodium sulfate (the dry basis quality of anhydrous sodium sulfate can be improved to 99%) can be produced.
The device for realizing the novel technology for preparing the alkali from the full brine comprises the following steps:
the invention provides a device for realizing a novel technology for preparing alkali from full brine, which comprises a brine reaction tank A1, a sedimentation tank B1, a nanofiltration membrane concentration and separation device C1, an evaporation concentration system and a centrifugal system which are sequentially communicated;
the evaporation concentration system comprises a first-effect evaporation concentration system D1 and a second evaporation concentration system D2, wherein:
the first-effect evaporation concentration system D1 is connected with a permeate outlet of the nanofiltration membrane concentration separation device C1 and is used for carrying out evaporation concentration crystallization treatment on permeate; a salt slurry outlet of the first-effect evaporation and concentration system D1 is sequentially communicated with a first centrifugal system F1 and a first drying device G1; a nitrate-poor residue discharge port of the first-effect evaporation concentration system D1 and a salt centrifugal mother liquor discharge port of the first centrifugal system F1 are communicated with an inlet of a nanofiltration membrane concentration and separation device C1;
the second-effect evaporation concentration system D2 is connected with a concentrated solution outlet of the nanofiltration membrane concentration separation device C1 and is used for carrying out evaporation concentration crystallization treatment on the concentrated solution; a salt slurry outlet of the second-effect evaporation and concentration system D2 is sequentially communicated with a second centrifugal system F2 and a second drying device G2; a nitrate-rich residue discharge port of the second-effect evaporation concentration system D2 and a nitrate centrifugal mother liquor discharge port of the second centrifugal system F2 are communicated with an inlet of a brine reaction tank A1;
as shown in fig. 1-5, the provided first-effect evaporation and concentration system D1 and second-effect evaporation and concentration system D2 have the same structure, collectively referred to as evaporation and concentration system, and include an evaporation kettle 1, wherein the evaporation kettle 1 is a reaction kettle conventionally used for evaporating a solvent in the prior art, the top of the evaporation kettle 1 has a feeding end, and the bottom of the evaporation kettle 1 has a discharging end, specifically, the evaporation kettle 1 includes a kettle body, the kettle body is provided with a jacket, the jacket is used for introducing hot steam to heat the kettle body, and the top of the kettle body is equipped with a stirring component to stir materials.
On the basis of the existing evaporation kettle 1, in order to increase the evaporation and concentration efficiency, the invention carries out the following structural improvement:
a plurality of evaporated liquid condensing assemblies 3 are communicated with the evaporation kettle 1; specifically, 6 evaporating liquid condensing assemblies 3 are communicated with an evaporation kettle 1; 6 evaporating liquid condensing assemblies 3 are distributed on the top of the evaporating kettle 1 in an annular array.
Evaporating liquid condensing unit 3 includes condensation kettle 31, the top intercommunication of evaporation kettle 1 has condenser pipe 2, condenser pipe 2 runs through condensation kettle 31's top, the intercommunication has two condensing mechanism 32 that upper and lower interval set up on condenser pipe 2. The condensing mechanisms 32 are all positioned in the condensing kettle 31. The condensing kettle 31 is a kettle body conventionally used for condensation disclosed in the prior art, and is provided with a jacket filled with frozen brine for cooling.
The condensing mechanism 32 comprises a condensing disc 322 communicated with the condensing pipe 2, a condensing cavity is arranged in the condensing disc 322, the outer side wall of the condensing disc 322 is communicated with a plurality of annular pipelines 321, a plurality of condensing balls 324 are annularly distributed on the annular pipelines 321, and the plurality of condensing balls 324 are distributed on the annular pipelines 321 in an upper layer and a lower layer; the outer side wall of the condensate tray 322 is communicated with a plurality of side end pipes 323, and the side end pipes 323 are communicated with the inner side wall of the annular pipeline 321. Meanwhile, the condensing ball 324 is disposed in inclined communication with the circular pipe 321. A plurality of the condensing balls 324 are distributed at the upper end and the lower end of the annular pipeline 321 in an annular array distribution mode; the condensing ball 324 is communicated with the annular pipeline 321 through a pipeline 3241; the condensing ball 324 at the upper end of the annular pipe 321 is arranged obliquely upwards, and the condensing ball 324 at the lower end of the annular pipe 321 is arranged obliquely downwards; the annular pipeline 321 is provided with a plurality of liquid discharge holes, condensed liquid flows out of the condensing mechanism 32 through the liquid discharge holes and is collected in the condensing kettle 31, and the condensing kettle 31 is provided with liquid outlet holes and a liquid outlet valve.
The evaporation concentration system of the new technology for preparing the total halogenated soda further comprises a vacuum component matched with the evaporated liquor condensation component 3, and vacuum is formed in the condensation kettle 31 through the vacuum component.
The vacuum assembly comprises an annular vacuum pipeline 4, and the annular vacuum pipeline 4 is communicated with the top of the condensation kettle 31 through a side pipeline 41 downwards; the annular vacuum pipeline 4 is communicated with a vacuum pump 42; meanwhile, a plurality of vacuum through holes 21 are formed in the condensation pipe 2, and the vacuum through holes 21 are located in the condensation kettle 31. The condensation pipe 2 is connected with a valve.
The specific process of the evaporation concentration system is as follows:
let in hot steam on evaporating pot 1 according to current mode, at this moment, the solvent molecule heating in the evaporating pot 1 forms steam, steam enters into condensing pot 31 respectively from 6 condenser pipe 2 in, at this moment, steam enters into in the lime set 322, enters into condensation ball 324 along side end pipe 323 from lime set 322 in (condensation ball 324 adopts glass material, inside has the cavity), realize increasing the condensation area through this mode, steam can be by abundant condensation.
Secondly, the vacuum assembly of condensation kettle 31 top intercommunication can realize, when needs decompression concentration, opens vacuum pump 42, all condensation kettle 31 mesomorphic vacuum, simultaneously, because of condenser pipe 2 passes through vacuum through-hole 21 and evaporation kettle 1 formation vacuum, and then realizes the decompression concentration of solvent.
As shown in fig. 7-8, the centrifugal system comprises a base 11A, a centrifugal system body 1A is assembled on the top of the base 11A (the centrifugal system body 1A is a conventional centrifugal system disclosed in the prior art and assembled on the top of the base 11A in the prior art), a shield assembly 2A is slidably connected on the base 11A, the shield assembly 2A comprises a shield 21A located right above the centrifugal system body 1A, and an annular protruding piece 23A is fixedly connected to the bottom edge portion of the shield 21A;
the annular protruding piece 23A is connected with two guide rods 22A in a sliding mode (rod holes matched with the guide rods 22A are formed in the annular protruding piece 23A), the two guide rods 22A are fixedly connected to the top of the base 11A, and the two guide rods 22A are distributed on the annular protruding piece 23A in a left-right symmetrical distribution mode.
The protective cover 21A is provided with two driving assemblies 3A (the two driving assemblies 3A are symmetrically arranged in front and back), the protective cover 21A is driven to move up and down through the driving assemblies 3A, and the centrifugal system body 1 is closed and opened through the up and down movement of the protective cover 21A;
the specific structure of each drive assembly 3A is as follows:
the driving assembly 3A includes a driving motor 32A disposed above the protection cover 21A;
the driving motor 32A is connected with a lead screw 31A downwards, and the annular lug 23A is fixedly connected with a lead screw barrel 311A in threaded connection with the lead screw 31A (the lead screw barrel 311A has an internal thread matched with the lead screw 31A and is fixed on the annular lug 23A in a penetrating way); the lead screw 31A is in threaded connection with a lead screw barrel 311A; the lower end of the lead screw 31A is located below the annular lug 23A. The middle of the driving motor 32A in the driving assembly 3A positioned at the front end and the two ends of the annular lug 23A is fixedly connected with a bracket, and the bracket is fixedly connected on the base 11A. The bracket comprises a horizontal end 41A fixedly connected between the driving motors 32A; the horizontal end 41A is vertically connected with a vertical end 42A, and the vertical end 42A is fixedly connected to the front and rear side walls of the base 11A.
Simultaneously, be equipped with a plurality of buffer structure on protection casing 21A's inside wall, through buffer structure buffer protection casing 21A covers when closing centrifugal system body 1A, buffers protection casing 21A's vibration.
The buffer structures each include an elastic protrusion 231A, a lower end of the elastic protrusion 231A is located at the bottom inside the protection cover 21A, and an upper end of the elastic protrusion 231A is located at the top inside the protection cover 21A. The bottom fixedly connected with a plurality of bracing piece of base 11, the bottom fixedly connected with supporting seat of bracing piece.
The specific process of the centrifugal system of the new technology for preparing the total halogen alkali comprises the following steps:
first, open centrifugal system body 1A, centrifugal system body 1A work, in order to realize that operating personnel and centrifugal system body 1A keep apart protection operating personnel, open every driving motor 32A (according to the present mode two driving motor 32A with series connection back electric connection on the power).
The driving motor 32A drives the lead screw 31A to rotate, and under the driving of the driving motor 32A, the protecting cover 21A is driven by the lead screw 31A downward to the protecting cover 21A to be covered on the centrifugal system body 1A (the protecting cover 21A has a cavity therein, which can accommodate the centrifugal system body 1A), and at this time, the elastic protrusion 231A (the elastic protrusion 231A is made of rubber material) on the inner side wall of the protecting cover 21A is extruded on the centrifugal system body 1A. The protective cover 21A is made of polyurethane material, and has high impact resistance and light weight.
After the protection cover 21A covers the centrifugal system body 1A, the elastic protrusions 231 on the inner side wall of the protection cover 21A are pressed on the centrifugal system body 1A, and then the vibration generated by the centrifugal system body 1A can be effectively buffered by the elastic protrusions 231A.
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 and improvements made within the spirit and principle of the present invention are intended to be included within the scope of the present invention.
Claims (5)
1. A preparation method of a new technology for preparing alkali by total halogen is characterized by comprising the following steps:
step 1) sequentially adding a sodium carbonate saturated solution and a sodium hydroxide saturated solution into raw brine, adjusting the pH to 10-11, then adding a polymeric flocculant under stirring, and after the flocculation and precipitation are finished, filtering to separate the flocculation and precipitation and remove metal ions such as calcium, magnesium and the like;
step 2) passing the separated and precipitated brine through a nanofiltration membrane concentration and separation device to obtain less Na 2 SO 4 The nitrate-poor solution and Na-rich solution 2 SO 4 The nitrate-rich solution;
step 3) Na reduction 2 SO 4 The lean nitrate solution enters a first-effect evaporation concentration system for evaporation concentration, the temperature of evaporation concentration is controlled to be 80-130 ℃, the pressure is 0.04-0.12 MPa, salt slurry is separated out, salt slurry and lean nitrate residues are obtained through filtration, and the salt slurry is subjected to centrifugal dehydration separation to obtain crystal salt and salt centrifugal mother liquor;
step 4) rich in Na 2 SO 4 The rich nitrate solution enters a second effect for evaporationEvaporating and concentrating in a concentration system, controlling the temperature of evaporation and concentration at 90-105 ℃ and the pressure at 0.05-0.07 MPa, separating out nitre slurry, filtering to obtain nitre slurry and nitre-rich residues, and centrifugally dewatering and separating the nitre slurry to obtain anhydrous sodium sulphate and nitre centrifugal mother liquor;
returning the salt centrifugal mother liquor and the poor nitrate residue to a nanofiltration membrane concentration and separation device for secondary separation treatment;
mixing the nitrate centrifugal mother liquor and the nitrate-rich residues with the original brine, and then carrying out secondary separation treatment;
the volume ratio of the raw brine to the saturated sodium carbonate solution to the saturated sodium hydroxide solution is (1000: 45-75): 45-75 parts of;
the volume ratio of the raw brine to the polymeric flocculant is 1000:0.1-0.3, and the polymeric flocculant comprises polymeric ferric sulfate, polyacrylamide or the combination of the polymeric ferric sulfate and the polyacrylamide.
2. The device for realizing the preparation method of claim 1 is characterized by comprising a brine reaction tank, a sedimentation tank, a nanofiltration membrane concentration and separation device, an evaporation concentration system, a filtration device and a centrifugal system which are sequentially communicated;
the evaporation concentration system comprises a first-effect evaporation concentration system and a second evaporation concentration system, wherein:
the first-effect evaporation concentration system is connected with a permeate outlet of the nanofiltration membrane concentration and separation device and is used for carrying out evaporation concentration crystallization treatment on permeate; a salt slurry outlet of the first-effect evaporation concentration system is communicated with the first filtering device, the first centrifugal system and the first drying device in sequence; the nitrate-poor residue discharge port of the first filtering device and the salt centrifugation mother liquor discharge port of the first centrifugal system are communicated with the inlet of the nanofiltration membrane concentration and separation device;
the second-effect evaporation concentration system is connected with a concentrated solution outlet of the nanofiltration membrane concentration separation device and is used for carrying out evaporation concentration crystallization treatment on the concentrated solution; a salt slurry outlet of the second-effect evaporation and concentration system is communicated with the second filtering device, the second centrifugal system and the second drying device in sequence; a nitrate-rich residue outlet of the second filtering device and a nitrate centrifugal mother liquor outlet of the second centrifugal system are communicated with an inlet of the brine reaction tank;
the evaporation concentration system comprises an evaporation kettle, and a plurality of evaporated liquid condensation assemblies are communicated with the evaporation kettle;
the evaporated liquid condensing assembly comprises a condensing kettle, the top of the evaporating kettle is communicated with a condensing pipe, the condensing pipe penetrates through the top of the condensing kettle, the condensing pipe is communicated with a plurality of condensing mechanisms, and the condensing mechanisms are positioned in the condensing kettle;
the condensing mechanism comprises a condensing disc communicated with a condensing pipe, a condensing cavity is formed in the condensing disc, the outer side wall of the condensing disc is communicated with a plurality of annular pipelines, a plurality of condensing balls are annularly distributed on the annular pipelines, and the plurality of condensing balls are distributed on the annular pipelines in an upper layer and a lower layer;
the condensing ball is obliquely communicated with the annular pipeline;
the evaporation concentration system of the new technology for preparing the total halogenated soda also comprises a vacuum component matched with the evaporated liquor condensation component, and vacuum is formed in the condensation kettle through the vacuum component;
the centrifugal system comprises a base, a centrifugal system body is assembled at the top of the base, a protective cover assembly is connected onto the base in a sliding mode, the protective cover assembly comprises a protective cover located right above the centrifugal system body, and an annular protruding piece is fixedly connected to the edge of the bottom of the protective cover;
the annular convex sheet is connected with a plurality of guide rods in a sliding manner, and the guide rods are fixedly connected to the top of the base;
the centrifugal system is characterized in that the protective cover is provided with a driving assembly, the driving assembly drives the protective cover to move up and down, and the centrifugal system body is covered and opened through the up-and-down movement of the protective cover;
be equipped with a plurality of buffer structure on the inside wall of protection casing, through buffer structure buffers the protection casing and covers when closing centrifugal system body on, the vibration of buffering protection casing.
3. The device of claim 2, wherein the evaporation kettle comprises a kettle body, a jacket is arranged on the kettle body, and the jacket is used for introducing hot steam to heat the kettle body;
the evaporation kettle is communicated with 6 evaporated liquid condensing assemblies;
the 6 evaporative liquid condensing assemblies are distributed on the top of the evaporation kettle in an annular array;
the condensing pipe is communicated with two condensing mechanisms which are arranged at intervals up and down.
4. The device according to claim 3, wherein the outer side wall of the condensate tray is communicated with a plurality of side end pipes, and the side end pipes are communicated with the inner side wall of the annular pipeline;
the plurality of condensation balls are distributed at the upper end and the lower end of the annular pipeline in an annular array distribution mode;
the condensing ball is communicated with the annular pipeline through a pipeline;
the condensing balls positioned at the upper end of the annular pipeline are obliquely arranged upwards, and the condensing balls positioned at the lower end of the annular pipeline are obliquely arranged downwards;
the vacuum assembly comprises an annular vacuum pipeline which faces downwards and is communicated with the top of the condensation kettle through a side pipeline;
the annular vacuum pipeline is communicated with a vacuum pump;
the condensation pipe is provided with a plurality of vacuum through holes, and the vacuum through holes are positioned in the condensation kettle;
the condenser pipe is connected with a valve.
5. The apparatus of claim 2, wherein the drive assembly comprises a drive motor disposed above the shield;
the driving motor is connected with a screw rod downwards, and a screw rod barrel in threaded connection with the screw rod is fixedly connected onto the annular convex plate;
the screw rod is in threaded connection with the screw rod barrel;
the lower end of the lead screw is positioned below the annular convex sheet;
the front end and the rear end of the annular lug are both provided with a driving component;
the middle of a driving motor in the driving assembly positioned at the front end and the two ends of the annular lug is fixedly connected with a bracket, and the bracket is fixedly connected to the base;
the bracket comprises a horizontal end fixedly connected between the driving motors;
the horizontal end is vertically connected with a vertical end which is fixedly connected to the front side wall and the rear side wall of the base;
the buffer structures comprise elastic bulges, the lower ends of the elastic bulges are positioned at the bottom in the protective cover, and the upper ends of the elastic bulges are positioned at the top in the protective cover;
the bottom fixedly connected with a plurality of bracing piece of base, the bottom fixedly connected with supporting seat of bracing piece.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102838134A (en) * | 2012-09-17 | 2012-12-26 | 广州新普利节能环保科技有限公司 | Sal prunella coproduction technology and device adopting sodium sulfate type bittern mechanical vapour recompression method |
| CN202936209U (en) * | 2012-09-17 | 2013-05-15 | 广州新普利节能环保科技有限公司 | Co-production device of salt and mirabilite by mirabilite-type brine mechanical vapor recompression method |
| CN109850920A (en) * | 2018-12-04 | 2019-06-07 | 中国中轻国际工程有限公司 | A kind of sal prunella system bittern evaporation production sal prunella technique |
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| CN212151642U (en) * | 2020-03-10 | 2020-12-15 | 广州新普利节能环保科技有限公司 | Device for realizing total brine alkali-making technology |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102838134A (en) * | 2012-09-17 | 2012-12-26 | 广州新普利节能环保科技有限公司 | Sal prunella coproduction technology and device adopting sodium sulfate type bittern mechanical vapour recompression method |
| CN202936209U (en) * | 2012-09-17 | 2013-05-15 | 广州新普利节能环保科技有限公司 | Co-production device of salt and mirabilite by mirabilite-type brine mechanical vapor recompression method |
| CN109850920A (en) * | 2018-12-04 | 2019-06-07 | 中国中轻国际工程有限公司 | A kind of sal prunella system bittern evaporation production sal prunella technique |
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