CN115006857A - Intermittent evaporative crystallization device and process adopting two-effect parallel evaporation - Google Patents
Intermittent evaporative crystallization device and process adopting two-effect parallel evaporation Download PDFInfo
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 176
- 230000008025 crystallization Effects 0.000 title claims abstract description 175
- 238000001704 evaporation Methods 0.000 title claims abstract description 33
- 230000008020 evaporation Effects 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims description 30
- 230000008569 process Effects 0.000 title claims description 26
- 230000000694 effects Effects 0.000 claims abstract description 18
- 238000011084 recovery Methods 0.000 claims abstract description 18
- 238000004094 preconcentration Methods 0.000 claims description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 46
- 239000007788 liquid Substances 0.000 claims description 40
- 238000003756 stirring Methods 0.000 claims description 24
- 238000002156 mixing Methods 0.000 claims description 15
- 238000007599 discharging Methods 0.000 claims description 9
- 230000007246 mechanism Effects 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 7
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 14
- 229960001763 zinc sulfate Drugs 0.000 description 14
- 229910000368 zinc sulfate Inorganic materials 0.000 description 14
- 239000013078 crystal Substances 0.000 description 8
- 230000002411 adverse Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 230000001105 regulatory effect Effects 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 3
- 238000006297 dehydration reaction Methods 0.000 description 3
- 230000009977 dual effect Effects 0.000 description 3
- 239000012452 mother liquor Substances 0.000 description 3
- 206010053615 Thermal burn Diseases 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229940118149 zinc sulfate monohydrate Drugs 0.000 description 2
- RNZCSKGULNFAMC-UHFFFAOYSA-L zinc;hydrogen sulfate;hydroxide Chemical compound O.[Zn+2].[O-]S([O-])(=O)=O RNZCSKGULNFAMC-UHFFFAOYSA-L 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000005394 sealing glass Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/02—Crystallisation from solutions
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G9/00—Compounds of zinc
- C01G9/06—Sulfates
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B37/00—Component parts or details of steam boilers
- F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
- F22B37/26—Steam-separating arrangements
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D11/00—Feed-water supply not provided for in other main groups
- F22D11/02—Arrangements of feed-water pumps
- F22D11/06—Arrangements of feed-water pumps for returning condensate to boiler
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- General Engineering & Computer Science (AREA)
- Crystallography & Structural Chemistry (AREA)
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Abstract
The invention relates to an intermittent evaporative crystallization device adopting two-effect parallel evaporation, which is characterized by comprising a first-effect crystallization tank internally provided with a first-effect steam coil, a second-effect crystallization tank internally provided with a second-effect steam coil, a raw steam recovery part and a centrifugal crystallization part, wherein the first-effect crystallization tank and the second-effect crystallization tank are both sealed tank bodies, a raw steam conveying pipe for introducing raw steam generated by an external boiler is arranged on the first-effect crystallization tank, and an air inlet of the first-effect steam coil is communicated with the external raw steam conveying pipe; a primary mixed steam pipe communicated with a steam coil pipe in the secondary crystallization tank is also arranged on the primary crystallization tank; an air outlet pipe of the raw steam recovery part is communicated with the primary mixed steam pipe, and an air inlet pipe is communicated with an outlet of the primary steam coil pipe; and the feed end of the centrifugal crystallization part is respectively communicated with the discharge ends of the first effect crystallizing tank and the second effect crystallizing tank through discharge bottom valves.
Description
Technical Field
The invention belongs to the technical field of chemical crystallization devices and processes, and particularly relates to a batch evaporative crystallization device and process adopting two-effect parallel evaporation.
Background
The zinc sulfate monohydrate product is mainly a product obtained after heating, concentrating and crystallizing the zinc sulfate solution, the existing zinc sulfate concentrating and crystallizing method mainly utilizes an open crystallization kettle to heat the zinc sulfate solution with steam so as to boil the zinc sulfate solution, and water in the solution is discharged from the crystallization kettle in a steam mode, so that the zinc sulfate solution is continuously concentrated and crystallized, and when the zinc sulfate monohydrate product is concentrated to meet the dehydration condition, centrifugal dehydration can be performed on the zinc sulfate solution, and the Yishui zinc sulfate product is obtained.
However, in the process of crystallizing zinc sulfate in an open crystallization kettle, secondary steam generated by heated solution and used raw steam can be directly discharged into the air and cannot be recycled, the raw steam is large in using amount and high in crystallization energy consumption, and meanwhile, the steam is discharged outside, so that a workshop scalding accident is easy to happen, and certain adverse effects can be caused on the surrounding environment;
in addition, because the open crystallization kettle is used for concentrating and crystallizing under the normal pressure condition, the speed of concentrating and crystallizing is low, the time consumption is long, and the efficiency of concentrating and crystallizing in unit time is low; meanwhile, when the zinc sulfate which meets the dehydration condition is discharged from the open crystallization kettle, the concentrated crystallization is in a stop state, and the concentrated crystallization cannot be continuously carried out, so that the crystallization time of the zinc sulfate is further prolonged, and the concentrated crystallization efficiency of the open crystallization kettle in unit time is low.
Disclosure of Invention
The invention aims to provide a device and a process for intermittent evaporative crystallization by adopting two-effect parallel evaporation, which are used for solving the technical problems that evaporative crystallization in the prior art is high in energy consumption, long in time consumption and low in efficiency, steam scald accidents are easy to happen, and the surrounding environment is affected by high temperature.
In order to achieve the purpose, the technical scheme adopted by the invention is as follows:
an intermittent evaporative crystallization device adopting two-effect parallel evaporation comprises a first-effect crystallization tank internally provided with a first-effect steam coil, a second-effect crystallization tank internally provided with a second-effect steam coil, a raw steam recovery part and a centrifugal crystallization part, wherein the first-effect crystallization tank and the second-effect crystallization tank are both sealed tank bodies, a raw steam conveying pipe for introducing raw steam generated by an external boiler is arranged on the first-effect crystallization tank, and an air inlet of the first-effect steam coil is communicated with the external raw steam conveying pipe;
a primary mixed steam pipe communicated with a steam coil pipe in the secondary crystallization tank is also arranged on the primary crystallization tank; an air outlet pipe of the raw steam recovery part is communicated with the primary mixed steam pipe, and an air inlet pipe is communicated with an outlet of the primary steam coil pipe;
and the feed end of the centrifugal crystallization part is respectively communicated with the discharge ends of the first effect crystallizing tank and the second effect crystallizing tank through discharge bottom valves.
The secondary mixed steam pipe is communicated with the air inlet end of the steam coil pipe in the pre-concentration tank;
and the air inlet pipe of the mixed steam recovery part is respectively communicated with the steam coil pipe in the secondary crystallization tank and the steam coil pipe in the preconcentration tank, and the air outlet pipe is communicated with the secondary mixed steam pipe.
The feed end of pre-concentration jar passes through finished product water inlet pipe and outside finished product water intercommunication, the discharge end of pre-concentration jar respectively through the pump body, liquid conveying line and set up the valve body on liquid conveying line with the feed inlet intercommunication of an effect crystallizer, two effect crystallizers.
And the first effect crystallizing tank, the second effect crystallizing tank and the pre-concentration tank are internally provided with stirring mechanisms.
The raw steam recovery part comprises a raw steam gas-liquid separator, the mixed steam recovery part comprises a mixed steam gas-liquid separator, and the condensed water outlet ends of the raw steam gas-liquid separator and the mixed steam gas-liquid separator are respectively communicated with an external steam boiler through steam condensed water pipes.
A batch evaporative crystallization process adopting two-effect parallel evaporation comprises the following process steps,
A. respectively injecting solutions to be crystallized into the tank bodies of the first-effect crystallizing tank and the second-effect crystallizing tank, conveying raw steam into the first-effect crystallizing tank, stirring the solutions in the first-effect crystallizing tank, and carrying out evaporative crystallization on the solutions;
B. recovering raw steam output from the primary crystallization tank, mixing the recovered raw steam with secondary steam generated in the evaporative crystallization process of the primary crystallization tank to form primary mixed steam, conveying the primary mixed steam into the secondary crystallization tank, stirring the solution in the secondary crystallization tank, and carrying out evaporative crystallization on the primary mixed steam;
C. discharging the solution in the first-effect crystallizing tank to a centrifugal crystallizing part after the concentration of the solution reaches 60-85 Baume degrees, and centrifuging to obtain a product;
D. and discharging the solution in the double-effect crystallizing tank to a centrifugal crystallizing part after the concentration of the solution reaches 60-85 Baume degrees, and centrifuging to obtain the product.
It also comprises the following steps of,
E. continuously injecting finished water into the pre-concentration tank, recovering primary mixed steam output from the secondary crystallization tank, mixing the recovered primary mixed steam with secondary steam generated in the evaporative crystallization process of the secondary crystallization tank to form secondary mixed steam, conveying the secondary mixed steam into the pre-concentration tank, stirring the finished water in the pre-concentration tank, and continuously pre-concentrating the finished water in the pre-concentration tank by using the secondary mixed steam;
F. after the pre-concentration of the finished product water reaches 30-55 Baume degrees, injecting the finished product water into a first-effect crystallizing tank or a second-effect crystallizing tank, and evaporating and crystallizing;
G. and E, recovering the secondary mixed steam output from the pre-concentration tank, mixing the recovered secondary mixed steam with the secondary mixed steam in the step E again, and conveying the mixed steam into the pre-concentration tank.
And the raw steam, the primary mixed steam and the secondary mixed steam are recovered after gas-liquid separation.
Adopt the produced beneficial effect of above-mentioned technical scheme to lie in:
according to the device and the process adopting two-effect parallel evaporation and intermittent evaporation crystallization, raw steam and secondary steam generated in the crystallization process are recovered and mixed into primary mixed steam and secondary mixed steam, and the primary mixed steam and the secondary mixed steam are put into the next crystallization tank or a preconcentration tank, so that the heat energy of the raw steam is fully utilized, the heat energy utilization rate of the primary raw steam is improved, the usage amount of the raw steam is obviously reduced, and the crystallization energy consumption is reduced in the evaporation crystallization process of the same amount of solution;
secondly, the sealed tank body is adopted for crystallization, the air pressure in the tank body is controlled to evaporate and crystallize in a specified pressure interval, a high-pressure environment is created for the solution in the first-effect crystallizing tank and the second-effect crystallizing tank, the evaporation and crystallization of the solution can be effectively accelerated, the evaporation and crystallization time of the solution under unit volume can be obviously shortened, and due to the fact that steam is prevented from being discharged outside, steam scald accidents can be effectively avoided, and adverse effects of the discharged steam on the surrounding environment are avoided;
in addition, in the process of recovering the raw steam, the primary mixed steam and the secondary mixed steam, gas-liquid separation is carried out on the raw steam, pure steam condensate water can be obtained through separation and is led into a boiler for generating the raw steam, the cyclic utilization of the raw steam and water in the solution can be realized, and the water source consumption is reduced.
According to the technical scheme provided by the invention, through recycling the steam, the energy contained in the raw steam and the secondary steam generated in the crystallization process is fully utilized, the heat energy utilization rate is high, the crystallization energy consumption is obviously reduced, the crystallization time is effectively shortened, the crystallization efficiency and the yield are improved, the production benefit of enterprises is improved, and the adverse effect of discharged hot steam on the environment can be effectively reduced due to the reduction of the steam discharged to the outside, so that the steam crystallization method is favorable for popularization and use in the field of chemical crystallization.
Drawings
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a process flow diagram of the present invention.
The notation in the figure is: 1. the device comprises a first-effect crystallizing tank, a second-effect crystallizing tank, a first-effect steam coil, a second-effect steam coil, a 303 pre-concentration steam coil, a 4 raw steam conveying pipe, a 5 primary mixing steam pipe, a 6 centrifugal machine, a 7 pre-concentration tank, a 8 secondary mixing steam pipe, a 9 finished product water feeding pipe, a 10 stirring mechanism, a 11 stirring motor, a 12 stirring paddle, a 13 raw steam gas-liquid separator, a 14 mixed steam gas-liquid separator, a 15 observation hole, a 16 discharging bottom valve, a 17 steam condensate pipe.
Detailed Description
For a better understanding of the objects, structure and function of the invention, reference should be made to the following detailed description taken in conjunction with the accompanying drawings.
In this embodiment, the evaporated and crystallized zinc sulfate is taken as an example, and the specific steps are as follows:
as shown in fig. 1, the invention provides an intermittent evaporative crystallization device adopting two-effect parallel connection, which comprises a first-effect crystallization tank 1 internally provided with a first-effect steam coil 301, a second-effect crystallization tank 2 internally provided with a second-effect steam coil 302, a raw steam recovery part and a centrifugal crystallization part, wherein the first-effect crystallization tank 1 and the second-effect crystallization tank 2 are both sealed tank bodies, so that the pressure in the first-effect crystallization tank 1 and the second-effect crystallization tank 2 is conveniently controlled within a specified range, a proper pressure environment is provided for evaporative crystallization of a solution, the speed of evaporative crystallization is accelerated, and the efficiency of evaporative crystallization is improved; one imitate and be equipped with the raw steam conveyer pipe 4 that lets in the raw steam that outside boiler produced on crystallizer 1, one imitate the air inlet of steam coil 301 and give birth to steam conveyer pipe 4 intercommunication outside, pour into the solution of treating the crystallization in one imitate crystallizer 1 after, to one imitate steam coil 301 of its inside let in raw steam, the solution of its inside is under the effect of the heat that contains of raw steam, the evaporation crystallization.
In addition, a primary mixed steam pipe 5 communicated with a secondary steam coil 302 in the secondary crystallization tank 2 is also arranged on the primary crystallization tank 1, and secondary steam generated in the crystallization process of the solution in the primary crystallization tank 1 is introduced into the secondary steam coil 302 through the primary mixed steam pipe 5; meanwhile, in order to recover the raw steam and the condensed water therein output from the single-effect crystallization tank 1 and fully utilize the heat in the raw steam, the raw steam recovery part in the embodiment comprises a raw steam gas-liquid separator 13 and other fittings such as pipelines and valves which are matched with the raw steam gas-liquid separator to work, an outlet pipe of the raw steam gas-liquid separator 13 is communicated with the primary mixed steam pipe 5 through a pipeline, an inlet pipe is communicated with an outlet of the single-effect steam coil 301 through a pipeline, the raw steam gas-liquid separator 13 is utilized to carry out gas-liquid separation on the recovered raw steam to obtain pure condensed water and raw steam, and the separated raw steam is introduced into the primary mixed steam pipe 5 to be mixed with secondary steam in the primary mixed steam pipe to form primary mixed steam for evaporating and crystallizing the solution in the double-effect crystallization tank 2.
Further, in order to facilitate leading out the residual solution and the crystals after the evaporation in the first-effect crystallization tank 1 and the second-effect crystallization tank 2 from the first-effect crystallization tank 1 and the second-effect crystallization tank 2, the feed ends of the centrifugal crystallization part are respectively communicated with the discharge ends of the first-effect crystallization tank 1 and the second-effect crystallization tank 2 through a discharge bottom valve 16, and the centrifugal crystallization part in this embodiment includes a centrifuge 6 and other accessories that cooperate with the centrifuge 6 to work.
Further, in order to recover the primary mixed steam output from the dual-effect crystallization tank 2 and fully utilize the heat in the primary mixed steam, the crystallization device further comprises a pre-concentration tank 7 internally provided with a pre-concentration steam coil 303 and a mixed steam recovery part, wherein a secondary mixed steam pipe 8 communicated with the air inlet end of the steam coil in the pre-concentration tank 7 is arranged on the dual-effect crystallization tank 2; the feed end of pre-concentration tank 7 passes through finished product water inlet pipe 9 and outside finished product water intercommunication, the discharge end of pre-concentration tank 7 respectively through the pump body, liquid conveying pipeline and set up the valve body on liquid conveying pipeline with the feed inlet intercommunication of crystallization tank 1, two effect crystallization tanks 2 is imitated to one.
The mixed steam recovery part comprises a mixed steam-liquid separator 14 and other accessories such as pipelines and valves which are matched with the mixed steam-liquid separator to work, wherein an air inlet pipe of the mixed steam-liquid separator 14 is respectively communicated with an air outlet of the two-effect steam coil 302 and an air outlet of the pre-concentration steam coil 303, and an air outlet pipe is communicated with the secondary mixed steam pipe 8. The mixed steam gas-liquid separator 14 is utilized to recover and separate gas and liquid from the primary mixed steam output from the two-effect steam coil 302 to obtain pure condensed water and primary mixed steam, and the separated primary mixed steam is introduced into the secondary mixed steam pipe 8 to be mixed with secondary steam in the secondary mixed steam pipe to form secondary mixed steam for pre-concentrating the finished water in the pre-concentration tank 7.
In addition, in order to provide a high-pressure crystallization environment for the solution in the tank, to increase the crystallization speed and shorten the crystallization time, in the present embodiment, the single-effect crystallization tank 1 and the double-effect crystallization tank 2 are provided as sealed type tanks, and pressure regulating valves are provided at the inlet of the primary mixing steam pipe 5 and the inlet of the secondary mixing steam pipe 8 to control the air pressures in the single-effect crystallization tank 1 and the double-effect crystallization tank 2, the opening pressure of the pressure regulating valve on the primary mixing steam pipe 5 is set to 0.35MPa, the opening pressure of the pressure regulating valve on the secondary mixing steam pipe 8 is set to 0.15MPa, and when the air pressures in the single-effect crystallization tank 1 and the double-effect crystallization tank 2 exceed 0.35MPa and 0.15MPa, respectively, the pressure regulating valves are opened, and the secondary steam in the single-effect crystallization tank 1 is input into the primary mixing steam pipe 5, and the secondary steam in the double-effect crystallization tank 2 is input into the secondary mixing steam pipe 8. And the arrangement that the first-effect crystallizing tank 1 and the second-effect crystallizing tank 2 are sealed tank bodies can also avoid the consequences of scalding workers and causing adverse effects on the surrounding environment due to the discharge of secondary steam.
Further, in order to promote evaporation and crystallization of the solution in the first-effect crystallization tank 1 and the second-effect crystallization tank 2 and promote preconcentration of the product water in the preconcentration tank 7, and the crystallized product sinks to the bottom, in this embodiment, stirring mechanisms 10 are respectively disposed in the first-effect crystallization tank 1, the second-effect crystallization tank 2 and the preconcentration tank 7, and each stirring mechanism 10 is respectively adapted to a corresponding tank body (where the tank body is a general name of the first-effect crystallization tank 1, the second-effect crystallization tank 2 and the preconcentration tank 7), and includes a stirring motor 11 disposed outside the tank body and a stirring paddle 12 disposed in the tank body, where the stirring motor 11 is in transmission connection with the stirring paddle 12, and the stirring speed is about 60 rpm and is used for stirring the solution or the product water.
Furthermore, the condensed water outlet ends of the raw steam gas-liquid separator 13 and the mixed steam gas-liquid separator 14 in the embodiment are respectively communicated with an external steam boiler through a steam condensed water pipe 17, and are used for guiding pure condensed water obtained by gas-liquid separation back to the boiler to generate steam again for evaporation crystallization, so that water in raw steam and water in solution are fully utilized, a water source is saved, and the consumption of external water is reduced.
Furthermore, in order to facilitate observing the liquid level in the crystallization tank and the crystallization condition of the solution, in this embodiment, observation holes 15 are respectively formed at the top of the first-effect crystallization tank 1 and the top of the second-effect crystallization tank 2, and sealing glass is arranged on the observation holes 15 to maintain the sealing type of the tank body.
Above-mentioned setting, the feeding that has realized one and imitate crystallizer 1 and two and imitate crystallizer 2 is parallelly connected and the raw steam is parallelly connected, solution concentration in one imitates crystallizer 1 is to satisfying the centrifugal condition and arrange surplus solution and crystal to centrifuge 6's in-process through blowing bottom valve 16, raw steam can last let in two imitate crystallizer 2 through raw steam recovery part, can continue the evaporation crystallization in two imitate crystallizer 2 promptly, do not receive the influence of one imitate crystallizer 1, therefore, the crystallization can be carried out uninterrupted in succession, thereby, further shortened the whole crystallization time to the solution of unit volume of device, crystallization efficiency is improved.
As shown in figure 2, the intermittent evaporative crystallization process adopting double-effect parallel evaporation comprises the following process steps:
A. respectively injecting solutions to be crystallized into the tank bodies of the first-effect crystallizing tank 1 and the second-effect crystallizing tank 2, when the solutions are injected to the height of 3/4 tank bodies in the tank bodies, starting to convey raw steam into the first-effect crystallizing tank 1, carrying out heat conduction on the solutions in the first-effect crystallizing tank 1 by the raw steam through the first-effect steam coil 301, stirring the solutions in the first-effect crystallizing tank 1 by the stirring mechanism 10, and carrying out evaporative crystallization on the solutions;
in order to enable the raw steam to complete the double-effect crystallization of the first-effect crystallization tank 1 and the double-effect crystallization tank 2 and not to cause excessive heat waste, the temperature range of the raw steam input into the first-effect crystallization tank 1 is controlled within 150 to 190 ℃, preferably, the temperature of the raw steam introduced into the first-effect crystallization tank 1 is about 170 ℃ and the pressure is about 0.6MPa in the embodiment;
B. raw steam and condensed water output from the primary steam coil 301 are recovered by a raw steam gas-liquid separator 13 and subjected to gas-liquid separation, the separated raw steam is input into a primary mixed steam pipe 5 and is mixed with secondary steam generated in the evaporative crystallization process of the primary crystallization tank 1 to form primary mixed steam, the primary mixed steam is conveyed into the secondary crystallization tank 2 through the primary mixed steam pipe 5 to perform evaporative crystallization on the solution in the secondary crystallization tank 2, and a stirring mechanism 10 stirs the solution in the secondary crystallization tank 2 for promoting the evaporative crystallization;
C. after the concentration of the solution in the first-effect crystallizing tank 1 reaches 60-85 Baume degrees, opening a discharging bottom valve 16, discharging the residual solution and crystallized crystals into a centrifugal machine 6 of a centrifugal crystallizing part, and starting and centrifuging the centrifugal machine 6 to obtain a zinc sulfate product; preferably, in the embodiment, when the crystallization concentration reaches 75 Baume degrees, the residual solution and crystals in the single effect crystallization tank 1 are discharged to the centrifuge 6;
D. after the concentration of the solution in the secondary crystallization tank 2 reaches 60-85 Baume degrees, opening a discharging bottom valve 16, discharging the residual solution and the crystallized crystals into a centrifugal machine 6 of a centrifugal crystallization part, and starting and centrifuging the centrifugal machine 6 to obtain a zinc sulfate product; preferably, in the present embodiment, when the crystallization concentration reaches 75 baume degrees, the solution and crystals remaining in the dual effect crystallization tank 2 are discharged to the centrifuge 6.
And D, centrifuging the residual solution and the crystallized crystals in the step C and the step D in a centrifugal machine to obtain zinc sulfate crystals and residual mother liquor, and collecting the separated mother liquor into an external mother liquor barrel through a pipeline.
In addition, the process in this embodiment further includes the following steps:
E. continuously injecting finished water into the pre-concentration tank 7, recovering primary mixed steam and condensed water output from the secondary steam coil 302 by using a mixed steam gas-liquid separator 14, inputting the separated primary mixed steam into a secondary mixed steam pipe 8, mixing the separated primary mixed steam with secondary steam generated in the evaporative crystallization process of the secondary crystallization tank 2 to form secondary mixed steam, conveying the secondary mixed steam into the pre-concentration tank 7 through the secondary mixed steam pipe 8, pre-concentrating the finished water in the pre-concentration tank 7, and stirring the finished water in the pre-concentration tank 7 by using a stirring mechanism 10 to promote the full performance of the pre-concentration;
F. after the pre-concentration of the product water in the pre-concentration tank 7 reaches 30-55 Baume degrees, outputting the concentrated product water to the first-effect crystallizing tank 1 or the second-effect crystallizing tank 2 through a pump body and a liquid conveying pipeline between the pre-concentration tank 7 and the first-effect crystallizing tank 1 or the second-effect crystallizing tank 2, and carrying out evaporative crystallization; preferably, in this embodiment, when the pre-concentration of the product water reaches 40 baume degree and the temperature reaches above 80 ℃, the pre-concentrated product water can be selectively delivered to the first-effect crystallization tank 1 or the second-effect crystallization tank 2 through the valves on the liquid delivery pipeline, the pump body and the liquid delivery pipeline;
G. and (4) recovering secondary mixed steam output from the pre-concentration tank 7, mixing the recovered secondary mixed steam with the secondary mixed steam in the step (E) through the mixed steam gas-liquid separator 14 and the secondary mixed steam pipe 8 again, and conveying the mixed steam into the pre-concentration tank 7, so that heat in the steam is completely and fully utilized.
It is to be understood that the present invention has been described with reference to certain embodiments, and that various changes in the features and embodiments, or equivalent substitutions may be made therein by those skilled in the art without departing from the spirit and scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the invention without departing from the essential scope thereof. Therefore, it is intended that the invention not be limited to the particular embodiment disclosed, but that the invention will include all embodiments falling within the scope of the appended claims.
Claims (8)
1. The utility model provides an adopt two effect evaporation intermittent type evaporation crystallization device that connects in parallel which characterized in that: the device comprises a first-effect crystallizing tank (1) internally provided with a first-effect steam coil pipe (301), a second-effect crystallizing tank (2) internally provided with a second-effect steam coil pipe (302), a raw steam recovery part and a centrifugal crystallizing part, wherein the first-effect crystallizing tank (1) and the second-effect crystallizing tank (2) are sealed tank bodies, a raw steam conveying pipe (4) for introducing raw steam generated by an external boiler is arranged on the first-effect crystallizing tank (1), and an air inlet of the first-effect steam coil pipe (301) is communicated with the external raw steam conveying pipe (4);
a primary mixed steam pipe (5) communicated with a steam coil pipe in the secondary crystallization tank (2) is also arranged on the primary crystallization tank (1); an air outlet pipe of the raw steam recovery part is communicated with the primary mixed steam pipe (5), and an air inlet pipe is communicated with an outlet of the primary steam coil pipe (301);
the feed end of the centrifugal crystallization part is respectively communicated with the discharge ends of the first-effect crystallization tank (1) and the second-effect crystallization tank (2) through a discharge bottom valve (16).
2. The intermittent evaporative crystallization device adopting the double-effect parallel evaporation as claimed in claim 1, wherein: the double-effect crystallization device is characterized by also comprising a pre-concentration tank (7) internally provided with a pre-concentration steam coil (303) and a mixed steam recovery part, wherein a secondary mixed steam pipe (8) communicated with the air inlet end of the pre-concentration steam coil (303) is arranged on the double-effect crystallization tank (2);
and an air inlet pipe of the mixed steam recovery part is respectively communicated with the two-effect steam coil (302) and the pre-concentration steam coil (303), and an air outlet pipe is communicated with the secondary mixed steam pipe (8).
3. The batch evaporative crystallization device adopting two-effect parallel evaporation as claimed in claim 2, wherein: the feed end of pre-concentration jar (7) passes through finished product water inlet pipe (9) and outside finished product water intercommunication, the discharge end of pre-concentration jar (7) respectively through the pump body, liquid conveying line and set up the valve body on liquid conveying line with the feed inlet intercommunication of an effect crystallizer (1), two effect crystallizer (2).
4. The batch evaporative crystallization device adopting two-effect parallel evaporation as claimed in claim 2, wherein: and stirring mechanisms (10) are arranged in the first-effect crystallizing tank (1), the second-effect crystallizing tank (2) and the pre-concentrating tank (7).
5. The batch evaporative crystallization device adopting two-effect parallel evaporation according to claim 2, characterized in that: the raw steam recovery part comprises a raw steam gas-liquid separator (13), the mixed steam recovery part comprises a mixed steam gas-liquid separator (14), and the condensed water outlet ends of the raw steam gas-liquid separator (13) and the mixed steam gas-liquid separator (14) are respectively communicated with an external steam boiler through steam condensate pipes (17).
6. A batch evaporative crystallization process adopting two-effect parallel evaporation is characterized in that: the process comprises the following steps of,
A. respectively injecting a solution to be crystallized into the tank bodies of the first-effect crystallizing tank (1) and the second-effect crystallizing tank (2), conveying raw steam into the first-effect crystallizing tank (1), stirring the solution in the first-effect crystallizing tank (1), and carrying out evaporative crystallization on the solution;
B. the raw steam output from the primary crystallization tank (1) is recovered, the recovered raw steam is mixed with secondary steam generated in the evaporation crystallization process of the primary crystallization tank (1) to form primary mixed steam, the primary mixed steam is conveyed into the secondary crystallization tank (2), the solution in the secondary crystallization tank (2) is stirred, and the primary mixed steam is used for evaporation crystallization;
C. after the concentration of the solution in the primary crystallization tank (1) reaches 60-85 Baume degrees, discharging the solution to a centrifugal crystallization part, and centrifuging to obtain a product;
D. and (3) after the concentration of the solution in the double-effect crystallization tank (2) reaches 60-85 Baume degrees, discharging the solution to a centrifugal crystallization part, and centrifuging to obtain the product.
7. The batch evaporative crystallization process using two-effect parallel evaporation according to claim 6, wherein: it also comprises the following steps of,
E. continuously injecting finished water into the pre-concentration tank (7), recovering primary mixed steam output from the secondary crystallization tank (2), mixing the recovered primary mixed steam with secondary steam generated in the evaporation crystallization process of the secondary crystallization tank (2) to form secondary mixed steam, conveying the secondary mixed steam into the pre-concentration tank (7), stirring the finished water in the pre-concentration tank (7), and continuously pre-concentrating the finished water in the pre-concentration tank (7) by using the secondary mixed steam;
F. after the pre-concentration of the finished product water reaches 30-55 Baume degrees, injecting the finished product water into a first-effect crystallizing tank (1) or a second-effect crystallizing tank (2), and evaporating and crystallizing;
G. and (D) recovering the secondary mixed steam output from the pre-concentration tank (7), mixing the recovered secondary mixed steam with the secondary mixed steam in the step (E) again, and conveying the mixed steam into the pre-concentration tank (7).
8. The batch evaporative crystallization process using two-effect parallel evaporation according to claim 7, wherein: and the raw steam, the primary mixed steam and the secondary mixed steam are recovered after gas-liquid separation.
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