CN211462090U - Evaporation concentration system for producing high-solid-content solution - Google Patents

Abstract

The utility model relates to an evaporative concentration system of production high solid content solution, it includes a plurality of evaporation unit that link to each other, still include the steam generation device of the evaporation unit connection with a plurality of links to each other, the comdenstion water collection device, vacuum pump and stoste charge pump, single evaporation unit is including heater and sedimentation separator, the lateral wall of heater is provided with steam inlet and comdenstion water export, sedimentation separator is including vaporization centrifugal chamber and the settling chamber that is located vaporization centrifugal chamber below, the lateral wall of vaporization centrifugal chamber is provided with the hot material import, the top of heater is provided with the hot material export, the lateral wall upper end of settling chamber is provided with the clear liquid export, the bottom of heater is provided with the clear liquid import, the top of vaporization centrifugal chamber is provided with the secondary steam export, the bottom of settling chamber is provided. The utility model discloses have the effect that the putty condition takes place among the reduction material evaporative concentration process.

Description

Evaporation concentration system for producing high-solid-content solution

Technical Field

The utility model belongs to the technical field of the evaporative concentration equipment and specifically relates to an evaporative concentration system of production high solid content solution is related to.

Background

Evaporative concentration generally refers to a process of heating a solution without non-volatility or low volatility to a certain temperature by heating, so that a part of the solvent with a low boiling point is vaporized and removed in advance, thereby increasing the concentration of solute in the solution. The process of evaporative concentration is widely used in the chemical industry, food industry and pharmaceutical industry.

In the prior art, a chinese utility model patent with publication number CN208877938U discloses a multiple-effect evaporation concentration system, which relates to the technical field of evaporation concentration to solve the technical problem of low energy utilization rate; the multi-effect evaporative concentration system of the present embodiment comprises: the first-effect evaporator and the first-effect steam-water separator are connected with the first-effect evaporator; the double-effect evaporator and the double-effect steam-water separator are connected with the double-effect evaporator; wherein, multiple-effect evaporation concentration system still includes: a first ejector and a second ejector; the first ejector is connected with a steam outlet of the first-effect steam-water separator in a butt joint mode, a first outlet of the first ejector is connected with a steam inlet of the first-effect evaporator in a butt joint mode, and a first drainage port of the first ejector is connected with a second inlet of the second ejector in a butt joint mode; a second ejector port of the second ejector is in butt joint with a steam outlet of the secondary-effect steam-water separator; the utility model discloses multiple-effect evaporation concentration system is through quantity and the position of rational configuration ejector to reduce the consumption to the energy, thereby improved the utilization efficiency of the energy.

The above prior art solutions have the following drawbacks: in the in-process of in-service use, at the concentrated later stage of evaporation, material concentration often is very high to lead to the material to produce the condition of putty when the heating pipe of evaporimeter easily, thereby influence the normal flow of material, this evaporative concentration efficiency that has not only reduced the material, still lead to the material pipe valve among the vaporization system to take place to damage simultaneously easily.

SUMMERY OF THE UTILITY MODEL

The utility model aims at providing an evaporative concentration system of production high solid content solution has the advantage that reduces the putty condition emergence among the material evaporative concentration process.

The above technical purpose of the present invention can be achieved by the following technical solutions:

an evaporation concentration system for producing high solid content solution comprises a plurality of evaporation units which are connected, and further comprises a steam generation device, a condensed water collection device, a vacuum pump and a stock solution feed pump which are connected with the plurality of evaporation units, wherein each evaporation unit comprises a heater and a sedimentation separator, the upper end of the side wall of the heater is provided with a steam inlet which is connected with the steam generation device, the lower end of the side wall of the heater is provided with a condensed water outlet which is connected with the condensed water collection device, the sedimentation separator comprises a vaporization chamber and a sedimentation chamber which is positioned below the vaporization centrifugal chamber, the side wall of the vaporization centrifugal chamber is provided with a hot material inlet, the top end of the heater is provided with a hot material outlet, a hot material pipeline is communicated between the hot material inlet and the hot material outlet, the upper end of the side wall of the sedimentation chamber is provided with a clear liquid outlet, and the bottom end, a clear liquid pipeline is arranged between the clear liquid outlet and the clear liquid inlet, a forced circulation pump is arranged on the clear liquid pipeline, a secondary steam outlet is arranged at the top end of the vaporization centrifugal chamber, and a discharge hole is arranged at the bottom end of the settling chamber.

By adopting the technical scheme, the material to be concentrated firstly enters from the clear liquid inlet at the bottom end of the heater, then generates heat exchange with hot steam in the heater and flows out from the hot material outlet, and enters the sedimentation separator through the hot material inlet along the hot material pipeline, the high-temperature material can generate secondary steam and gushes out from the secondary steam outlet at the top end of the vaporization centrifugal chamber, and then can be continuously recycled, and the residual material is subjected to centrifugal separation in the centrifugal chamber and flows into the sedimentation chamber for sedimentation separation. The heavier part of the material is gathered at the bottom of the settling chamber and gradually reaches the discharging requirement. Clear liquid on the upper layer in the settling chamber continuously overflows into the heater from the clear liquid outlet, materials which can be concentrated and recovered still exist in the clear liquid on the upper layer, but the concentration of the materials is low, and the generation of scaling on the inner wall of the pipeline of the heater can be effectively reduced after low-concentration materials enter the heater, so that the blocking condition of the heater is effectively reduced. And the materials circularly flow between the sedimentation separator and the heater for repeated concentration, so that the concentration degree of the materials can be effectively improved.

The utility model discloses further set up to, the centrifugal chamber of vaporization includes the vaporization section and connects the centrifugal section that sets up at the vaporization section lower extreme, the hot material import sets up the juncture at vaporization section and centrifugal section, the incoming direction of hot material import and the tangential direction coincidence of centrifugal section radial cross section, the end of centrifugal section inserts and sets up in the setting chamber and the internal diameter of centrifugal section evenly reduces from top to bottom.

By adopting the technical scheme, the feeding direction of the hot material inlet is coincided with the tangential direction of the radial section of the centrifugal section, so that the material can spirally descend along the inner wall of the centrifugal section after entering the vaporization centrifugal chamber, a liquid film is formed on the inner wall of the centrifugal section, in the flowing process, components with different weights in the material are quickly separated under the action of centrifugal force and are layered in the settling chamber to form concentrate slurry with higher solid content at the bottom of the settling chamber, and clear liquid with lower solid content above the slurry is formed.

The utility model discloses further set up to, the inner wall of settling chamber is provided with a plurality of stationary flow ring boards, and is a plurality of the stationary flow ring board is arranged along the direction of height of settling chamber and is set up, the stationary flow ring board is close to and has the circulation clearance between the border of centrifugation section and the outer wall of centrifugation section in advance, the clear solution export is located the top of the most top stationary flow ring board.

By adopting the technical scheme, when the materials fall into the settling chamber from the centrifugal section, the existing materials in the settling chamber are easily impacted, so that the separated materials in the settling chamber become more turbid. Through setting up the stationary flow ring board, can effectively reduce the disturbance phenomenon that the material received external influence and produced in the settling chamber to make the material of settling separation more stable in the settling chamber, thereby improve the settling chamber to the concentrated effect of material. The arrangement of the flow gaps can reduce the blocking influence of the flow stabilizing ring plate on the material flow in the settling chamber.

The utility model discloses further set up as, the top of vaporization centrifugal chamber is provided with the silk screen demister.

Through adopting above-mentioned technical scheme, the material constantly collides with the interior wall of vaporization centrifuge chamber and self between at centrifugal separation's in-process to make and be full of a lot of liquid drops in the space of vaporization chamber, the liquid drop that these collisions produced splashes away from in the secondary steam export easily, thereby leads to the material to run off or causes secondary pollution to other equipment in the evaporation process. For reducing the emergence of this condition, be provided with the silk screen demister, the gas that includes the liquid drop is when the silk screen demister, and the liquid drop receives stopping of silk screen demister to assemble into big liquid drop on the surface of silk screen demister, drops to the settling chamber afterwards to make the liquid drop content in the gas significantly reduce, improved the purity of secondary steam, also reduced material loss.

The utility model discloses further set up to, the bottom of settling chamber is provided with the concentrate and collects the section, concentrate export and concentrate backward flow mouth have been seted up on the concentrate section respectively, the intercommunication is provided with the concentrate pipeline between concentrate export and the concentrate backward flow mouth, be provided with ejection of compact circulating pump on the concentrate pipeline, the discharge gate sets up between ejection of compact circulating pump and concentrate backward flow mouth, discharge gate department is provided with the regulation formula bleeder valve.

Through adopting above-mentioned technical scheme, the material is at the concentrated in-process of circulation, and its concentrated material constantly piles up in the bottom of deposit room, and the condition of jam takes place for a long time after the easy bottom of deposit room, and a large amount of material adhesion lead to flowing the difficulty at the deposit room inner wall to make the concentrated material be difficult to take out. Set up ejection of compact circulating pump through here, can be so that the concentrate of settling chamber bottom constantly circulates between concentrate pipeline and settling chamber to reduce the emergence of material at the settling chamber inner wall adhesion scale deposit condition. When the concentrated material in the settling chamber reaches the setting accumulation volume, the staff can control regulation formula discharging valve and open to make the concentrated material of circulation flow out from the discharge gate, the concentrated material that flows out from the discharge gate can directly be as the finished product, or get into in other equipment and carry out further evaporation concentration.

The utility model discloses further set up to, the top of vaporization section is provided with temperature sensor and pressure sensor, the juncture of vaporization section and centrifugation section is provided with level sensor, the equal electricity of temperature sensor, pressure sensor and level sensor is connected with the PLC controller, the equal electricity of forced circulation pump, ejection of compact circulating pump and the regulation formula bleeder valve in PLC controller and each evaporation unit is connected.

By adopting the technical scheme, the temperature sensor and the pressure sensor are mainly used for measuring the steam pressure and the steam temperature in the vaporization section, when the temperature and the pressure of the secondary steam separated from the vaporization section are insufficient, the flow of the forced circulation pump needs to be properly improved through the PLC, the material amount entering the vaporization centrifugal chamber is improved, and therefore the temperature and the air pressure of the secondary steam are improved. Level sensor mainly is used for piling up the volume of material in settling chamber and the vaporization centrifugal chamber and measuring, generally speaking, the position of material should be less than the position of hot material import in the settling chamber, if the liquid level of material is too high, then probably there is the material to pile up in the evaporation unit, lead to the unable timely discharge of material, need come the flow that suitably improves ejection of compact circulating pump through the PLC controller this moment, and open regulation formula bleeder valve, make the material of piling up in the settling chamber in time discharge. If the liquid level sensor senses that the liquid level is at an overhigh level for a long time, the staff need to timely stop the evaporation unit for maintenance, and the accumulated materials are manually processed to ensure that the whole evaporation system stably and safely operates.

The utility model discloses further set up as, the evaporation unit is imitated for the ejection of compact to the direct evaporation unit that links to each other of steam inlet and the steam generation device of heater, the evaporation unit that the hot material import of sedimentation separator and stoste charge pump are direct links to each other is the feed effect evaporation unit, all the other evaporation unit is imitated for the centre, and the steam inlet of the heater in the evaporation unit is imitated to the centre and feed effect evaporation unit links to each other with the secondary steam export of the evaporation unit is imitated to the previous time, is provided with the feed supplement mouth on the clear solution pipeline in the evaporation unit is imitated to the centre evaporation unit and the ejection of compact, the feed supplement mouth sets up between forced circulation pump and clear solution export, each the feed supplement mouth links to each other with the discharge gate of the evaporation unit is imitated to.

Through adopting above-mentioned technical scheme, in whole evaporation process, often can't once only reach required evaporation effect by an evaporation unit alone, so in traditional handicraft, generally can establish ties a plurality of evaporation units, treat concentrated material and be used for evaporation concentration's steam from same direction each evaporation unit of passing through in proper order, reach multistage concentrated effect, in concentration process, the solid content of material crescent, and the secondary steam temperature in each evaporation unit then is constantly descending. In the evaporation process of the high-solid-content material, the self flowability of the material is sharply reduced after the material is concentrated, and the temperature of secondary steam is insufficient, so that the blockage is easy to occur when the secondary steam flows in a heater. Therefore, the evaporation concentration system adopts a mode of reverse flow of steam and materials for evaporation concentration, the evaporation concentration system comprising three evaporation units is taken as an example to illustrate the material flow direction in the evaporation concentration system, the materials enter the feeding effect evaporation unit from the stock solution feeding pump for evaporation concentration, after reaching a certain concentration, the materials flow out of the discharge port of the feeding effect evaporation unit and enter the material supplementing port of the middle effect evaporation unit, then flow into the heater of the middle effect evaporation unit for evaporation concentration, after the materials are evaporated and concentrated to a certain concentration in the middle effect evaporation unit, the materials enter the heater of the discharging effect evaporation unit through the discharge port of the middle effect evaporation unit for evaporation concentration, and the final required concentration of the materials can be reached in the primary evaporator.

Taking an evaporation concentration system comprising three evaporation units as an example, the steam flow direction in the evaporation concentration system is described, high-temperature and high-pressure saturated steam is generated in a steam generating device and directly flows into a heater of a discharging effect evaporation unit to perform heat exchange with materials, then secondary steam separated from a settling separator of the discharging effect evaporation unit flows out from a secondary steam outlet and flows into the heater of an intermediate effect evaporation unit to be used as a heat source of the heater, and then secondary steam separated from the settling separator of the intermediate effect evaporation unit flows out from the secondary steam outlet and flows into the heater of a feeding effect evaporation unit to be used as the heat source of the heater.

Therefore, the steam temperature and the steam pressure in the discharging-effect evaporation unit, the middle-effect evaporation unit and the feeding-effect evaporation unit are gradually reduced, correspondingly, the highest temperature which can be reached by the materials in each evaporation unit is also gradually reduced, and the material concentration in the discharging-effect evaporation unit, the middle-effect evaporation unit and the feeding-effect evaporation unit is also gradually reduced due to the flow direction of the materials. The high-concentration material can obtain better fluidity at higher temperature, and the problem of blockage caused by the increase of the material concentration is effectively solved, so that the operation of the whole evaporation concentration process is more stable.

The utility model discloses further set up to, the intercommunication is provided with the stoste inlet pipe between the evaporation unit's hot material import is imitated to stoste charge pump and feeding, the last connection of stoste inlet pipe is provided with the pre-heater, the secondary steam export in the evaporation unit is imitated with the feeding to the pre-heater links to each other.

Through adopting above-mentioned technical scheme, under the lower circumstances of ambient temperature, the mobility of material itself can become very poor, takes place to block up very easily when getting into the feeding and imitate the evaporation unit, so set up the pre-heater, heat the material under the normal atmospheric temperature to reentrant the heater that gets into in the feeding imitate the evaporation unit and carry out the evaporative concentration after the suitable temperature. The heat source of the preheater is from the secondary steam generated in the feeding effect evaporation unit, so that the energy utilization rate can be effectively improved, and the energy consumption is reduced.

The utility model discloses further set up to, still be provided with the swirler on the concentrate pipeline in the evaporation unit is imitated in the ejection of compact, the swirler is including tangential feed inlet and overflow mouth, the setting of swirler is imitated between ejection of compact circulating pump and the concentrate backward flow mouth in the evaporation unit in the ejection of compact, through concentrate pipe connection between overflow mouth and the concentrated feed back mouth, through concentrate pipe connection between tangential feed inlet and the ejection of compact circulating pump, the discharge gate setting that evaporation unit was imitated in the ejection of compact is in the bottom of swirler.

Through adopting above-mentioned technical scheme, the material in the deposit room in the evaporation unit is imitated in the ejection of compact probably takes place to mix when flowing out with the supernatant between to lead to final product can't reach required concentration. Through setting up the swirler, utilize centrifugal separation's mode to carry out further centrifugal concentration to the concentrated material in the evaporation unit is imitated in the ejection of compact to further improve material concentration.

To sum up, the utility model discloses following beneficial effect has:

1. through the arrangement of the vaporizing centrifugal chamber and the settling chamber, the effects of relieving material blockage and improving the concentration degree of the material can be achieved;

2. the temperature sensor, the pressure sensor and the liquid level sensor are arranged, so that the effect of realizing automatic control of the flow of materials and steam can be achieved;

3. through material and the setting of steam reverse flow, can play the effect that further reduces the material jam condition.

Drawings

FIG. 1 is a schematic diagram showing the overall configuration of an evaporative concentration system for producing a high-solid content solution according to this embodiment.

Fig. 2 is an enlarged schematic view of a portion a in fig. 1.

Fig. 3 is an enlarged schematic view of a portion B in fig. 1.

Fig. 4 is a schematic view of the internal structure of the settling separator in this embodiment.

In the figure, 1, an evaporation unit; 11. a discharging effect evaporation unit; 12. an intermediate effect evaporation unit; 13. a feed effect evaporation unit; 2. a heater; 21. a steam inlet; 22. a condensed water outlet; 23. a hot material outlet; 24. a hot material pipe; 25. a clear liquid inlet; 26. a clear liquid pipe; 261. a forced circulation pump; 262. a material supplementing port; 3. a settling separator; 31. a vaporizing centrifugal chamber; 311. a vaporization section; 3111. a hot material inlet; 3112. a secondary steam outlet; 3113. a temperature sensor; 3114. a pressure sensor; 312. a centrifugation section; 313. a wire mesh demister; 314. a liquid level sensor; 32. a settling chamber; 321. a clear liquid outlet; 322. a flow stabilizing ring plate; 33. a concentrated material collection section; 331. a concentrated material outlet; 332. a concentrate return port; 333. a concentrate line; 3331. a discharge circulating pump; 3332. a discharge port; 3333. an adjustable discharge valve; 4. a steam generating device; 5. a condensed water collecting device; 6. a vacuum pump; 7. a stock solution feed pump; 71. a stock solution feeding pipe; 72. a preheater; 8. a swirler; 81. a tangential feed inlet; 82. an overflow port.

Detailed Description

The present invention will be described in further detail with reference to the accompanying drawings.

Referring to fig. 1 and fig. 2, for the utility model discloses an evaporative concentration system of production high solid content solution, including a plurality of evaporation unit 1 that link to each other, still including the steam generation device 4, the comdenstion water collection device 5, vacuum pump 6 and the stoste charge pump 7 of being connected with a plurality of evaporation unit 1 among the evaporation system, single evaporation unit 1 is including interconnect's heater 2 and sedimentation separator 3, and in this embodiment, each heater 2 is heat transfer area is 43 square meters's shell and tube heat exchanger. The upper end of the side wall of the heater 2 is provided with a steam inlet 21, the steam inlet 21 is connected with a steam generating device 4, the lower end of the side wall of the heater 2 is provided with a condensed water outlet 22, the condensed water outlet 22 is connected with a condensed water collecting device 5, the sedimentation separator 3 comprises a vaporizing centrifugal chamber 31 and a sedimentation chamber 32, the sedimentation chamber 32 is connected below the vaporizing centrifugal chamber 31, the side wall of the vaporizing centrifugal chamber 31 is provided with a hot material inlet 3111, the top end of the heater 2 is provided with a hot material outlet 23, a hot material pipeline 24 is communicated between the hot material inlet 3111 and the hot material outlet 23, the upper end of the side wall of the sedimentation chamber 32 is provided with a clear liquid outlet 321, the bottom end of the heater 2 is provided with a clear liquid inlet 25, a clear liquid pipeline 26 is arranged between the clear liquid outlet 321 and the clear liquid inlet 25, a forced circulation pump 261.

Referring to fig. 2, the bottom of settling chamber 32 is provided with concentrate collection section 33, concentrate export 331 and concentrate backward flow mouth 332 have been seted up on the concentrate collection section 33 respectively, the intercommunication is provided with concentrate pipeline 333 between concentrate export 331 and the concentrate backward flow mouth 332, be provided with ejection of compact circulating pump 3331 on the concentrate pipeline 333, be provided with discharge gate 3332 on the concentrate pipeline 333, discharge gate 3332 sets up between ejection of compact circulating pump 3331 and concentrate backward flow mouth 332, discharge gate 3332 department is provided with regulation formula bleeder valve 3333.

Referring to fig. 1 and 2, the evaporation unit 1 includes three types, which are respectively a discharging effect evaporation unit 11, an intermediate effect evaporation unit 12 and a feeding effect evaporation unit 13, the evaporation unit 1 in which the steam inlet 21 is directly connected to the steam generating device 4 is the discharging effect evaporation unit 11, the evaporation unit 1 in which the hot material inlet 3111 is directly connected to the stock solution feeding pump 7 is the feeding effect evaporation unit 13, the rest of the evaporation units 1 located between the discharging effect evaporation unit 11 and the feeding effect evaporation unit 13 are intermediate effect evaporation units 12, steam inlets 21 in the intermediate effect evaporation units 12 and the feeding effect evaporation units 13 are connected with a second-stage steam outlet of the previous effect evaporation unit 1, clear liquid pipelines 26 in the intermediate effect evaporation units 12 and the feeding effect evaporation units 13 are provided with material supplementing ports 262, the material supplementing ports 262 are arranged between the forced circulation pump 261 and the clear liquid outlet 321, and each material supplementing port 262 is connected with a material outlet 3332 of the next effect evaporation unit 1. In this embodiment, the direction from the feeding effect evaporation unit 13 to the discharging effect evaporation unit 11 is front, and vice versa. The raw liquid feeding pump 7 is communicated with the hot material inlet 3111 of the feeding effect evaporation unit 13 to form a raw liquid feeding pipe 71, the raw liquid feeding pipe 71 is provided with a preheater 72, in the embodiment, the preheater 72 is a tubular preheater 72 with a heat exchange area of 10 square meters, the preheater 72 is connected with a secondary steam outlet 3112 of the feeding effect evaporation unit 13, and a heat source of the preheater 72 is from secondary steam generated in the feeding effect evaporation unit 13, so that the energy utilization rate can be effectively improved, and the energy consumption is reduced.

Referring to fig. 1 and fig. 3, a cyclone 8 is disposed on a concentrate pipeline 333 in the discharging effective evaporation unit 11, the cyclone 8 includes a tangential feed port 81 and an overflow port 82, the cyclone 8 is disposed between a discharging circulating pump 3331 and a concentrated feed back port in the discharging effective evaporation unit 11, the overflow port 82 is connected with the concentrated feed back port through the concentrate pipeline 333, the tangential feed port 81 is connected with the discharging circulating pump 3331 through the concentrate pipeline 333, and a discharge port 3332 in the discharging effective evaporation unit 11 is disposed on the cyclone 8 and located at the bottom end of the cyclone 8. Through setting up swirler 8, can utilize centrifugal separation's mode to carry out further centrifugal concentration to the concentrated material in ejection of compact effect evaporation unit 11 to further improve material concentration.

Referring to fig. 2 and 4, the vaporizing centrifugal chamber 31 includes a vaporizing section 311 and a centrifugal section 312 connected to and disposed at a lower end of the vaporizing section 311, a hot material inlet 3111 is disposed at a junction of the vaporizing section 311 and the centrifugal section 312, a feeding direction of the hot material inlet 3111 coincides with a tangential direction of a radial cross section of the centrifugal section 312, a terminal of the centrifugal section 312 is inserted and disposed in the settling chamber 32, and an inner diameter of the centrifugal section 312 is uniformly reduced from top to bottom. The feeding direction of the hot material inlet 3111 coincides with the tangential direction of the radial cross section of the centrifugal section 312, so that the material can spirally descend along the inner wall of the centrifugal section 312 after entering the vaporizing centrifugal chamber 31, and a liquid film is formed on the inner wall of the centrifugal section 312, during the flowing process, various components with different weights in the material are rapidly separated under the action of centrifugal force and are layered in the settling chamber 32, and a material concentrate slurry with high solid content located at the bottom of the settling chamber 32 is formed, and a clear liquid with low solid content located above the slurry is formed.

Referring to fig. 2 and 4, the inner wall of the settling chamber 32 is provided with a plurality of flow stabilizing ring plates 322, the plurality of flow stabilizing ring plates 322 are arranged along the height direction of the settling chamber 32, a flow gap is reserved between the edge of the flow stabilizing ring plate 322 close to the centrifugal section 312 and the outer wall of the centrifugal section 312, a clear liquid outlet 321 is located above the uppermost flow stabilizing ring plate 322, and the top end of the vaporizing centrifugal chamber 31 is provided with a wire mesh demister 313. When material falls from the centrifugal section 312 into the settling chamber 32, it is likely to impact the material already in the settling chamber 32, thereby causing the material already separated in the settling chamber 32 to become more cloudy. Through setting up stationary flow ring board 322, can effectively reduce the disturbance phenomenon that the material received external influence and produced in the settling chamber 32 to make the material that has subsided the separation in the settling chamber 32 more stable, thereby improve the concentration effect of settling chamber 32 to the material. The provision of the flow gap reduces the obstruction effect of the flow stabilizer plate 322 on the flow of material in the settling chamber 32. The material continuously collides with the inner wall of the vaporizing centrifugal chamber 31 and the vaporizing centrifugal chamber in the centrifugal separation process, so that the space of the vaporizing chamber is filled with a plurality of liquid drops, and the liquid drops generated by the collisions are easy to splash out from the secondary steam outlet 3112, thereby causing material loss or causing secondary pollution to other equipment in the evaporation process. In order to reduce the occurrence of the situation, the wire mesh demister 313 is arranged, and when the gas containing liquid drops passes through the wire mesh demister 313, the liquid drops are blocked by the wire mesh demister 313 and are converged into large liquid drops on the surface of the wire mesh demister 313, and then the large liquid drops drop into the settling chamber 32, so that the content of the liquid drops in the gas is greatly reduced, the purity of secondary steam is improved, and the material loss is also reduced. The top of the vaporization section 311 is provided with a temperature sensor 3113 and a pressure sensor 3114, the junction of the vaporization section 311 and the centrifugal section 312 is provided with a liquid level sensor 314, the temperature sensor 3113, the pressure sensor and the liquid level sensor 314 are all electrically connected with a PLC controller (not shown in the figure), and the PLC controller is electrically connected with a forced circulation pump 261, a discharge circulation pump 3331 and an adjustable discharge valve 3333 in each evaporation unit 1.

The implementation principle of the embodiment is as follows: the material to be concentrated enters from the clear liquid inlet 25 at the bottom end of the heater 2, then exchanges heat with the hot steam in the heater 2 and flows out from the hot material outlet 23, enters into the sedimentation separator 3 through the hot material inlet 3111 along the hot material pipeline 24, the high-temperature material generates secondary steam and flows out from the secondary steam outlet 3112 at the top end of the vaporizing centrifugal chamber 31, and then can be recycled continuously, and the rest material is centrifuged in the centrifugal chamber and flows into the sedimentation chamber 32 for sedimentation separation. The heavier parts of the material are collected at the bottom of the settling chamber 32 and gradually reach the discharge requirement. The clear liquid on the upper layer in the settling chamber 32 continuously overflows from the clear liquid outlet 321 to the heater 2, the materials which can be concentrated and recovered still exist in the clear liquid on the upper layer, but the concentration of the materials is low, and the generation of the scaling condition of the inner wall of the pipeline of the heater 2 can be effectively reduced after the low-concentration materials enter the heater 2, so that the blocking condition of the heater 2 is effectively reduced. And the materials circularly flow between the sedimentation separator 3 and the heater 2 for repeated concentration, so that the concentration degree of the materials can be effectively improved. The material is at the concentrated in-process of circulation, and its concentrate is constantly piled up in the bottom of settling chamber 32, and the condition of jam takes place for a long time after the easy settling chamber 32 bottom, and a large amount of materials adhesion leads to flowing the difficulty at settling chamber 32 inner wall to make the concentrate difficult to take out. Through setting up ejection of compact circulating pump 3331 here, can make the concentrate of settling chamber 32 bottom constantly circulate between concentrate pipeline 333 and settling chamber 32 to reduce the emergence of material at the adhesion scale deposit condition of settling chamber 32 inner wall. When the concentrated material in the settling chamber 32 reaches the set accumulation amount, the PLC controller automatically controls the adjustable discharge valve 3333 to open, and the circulating concentrated material flows out from the discharge port 3332, and the concentrated material flowing out from the discharge port 3332 can be directly used as a finished product or enter other equipment for further treatment.

In whole evaporation process, often can't once only reach required evaporation effect by an evaporation unit 1, so in traditional handicraft, generally can establish ties a plurality of evaporation units 1, treat concentrated material and the steam that is used for evaporation concentration and pass through each evaporation unit 1 in proper order from same direction, reach multistage concentrated effect, in concentration process, the solid content of material crescent, and the secondary steam temperature in each evaporation unit 1 then is constantly descending. In the evaporation process of the high solid content material, the fluidity of the material itself is sharply reduced after the concentration, and the temperature of the secondary steam is insufficient, thereby causing a situation that the blockage is easily generated when the secondary steam flows in the heater 2. Therefore, the evaporation concentration system adopts a mode of reverse flow of steam and materials for evaporation concentration, taking an evaporation concentration system comprising three evaporation units 1 as an example, the material flow direction in the evaporation concentration system is described, the material enters the feeding effect evaporation unit 13 from the stock solution feeding pump 7 for evaporation concentration, after reaching a certain concentration, the material flows out of the discharge port 3332 of the feeding effect evaporation unit 13 and enters the material supplementing port 262 of the intermediate effect evaporation unit 12, then flows into the heater 2 of the intermediate effect evaporation unit 12 for evaporation concentration, after being evaporated and concentrated to a certain concentration in the intermediate effect evaporation unit 12, the material enters the heater 2 of the discharge effect evaporation unit 11 through the discharge port 3332 of the intermediate effect evaporation unit 12 for evaporation concentration, and the final required concentration of the material can be reached in the primary effect evaporator.

Taking an evaporation concentration system comprising three evaporation units 1 as an example, the steam flow direction in the evaporation concentration system is described, high-temperature and high-pressure saturated steam is generated in the steam generating device 4 and directly flows into the heater 2 of the discharging effect evaporation unit 11 to perform a heat exchange effect with materials, then secondary steam separated in the sedimentation separator 3 of the discharging effect evaporation unit 11 flows out from the secondary steam outlet 3112 and flows into the heater 2 of the intermediate effect evaporation unit 12 to be used as a heat source of the heater 2, and then secondary steam separated in the sedimentation separator 3 of the intermediate effect evaporation unit 12 flows out from the secondary steam outlet 3112 and flows into the heater 2 of the feeding effect evaporation unit 13 to be used as a heat source of the heater 2.

It can be seen that the steam temperature and the steam pressure in the discharging-effect evaporation unit 11, the intermediate-effect evaporation unit 12 and the feeding-effect evaporation unit 13 are gradually reduced, correspondingly, the highest temperature that can be reached by the material in each evaporation unit 1 is also gradually reduced, and the material concentration in the discharging-effect evaporation unit 11, the intermediate-effect evaporation unit 12 and the feeding-effect evaporation unit 13 is also gradually reduced due to the flow direction of the material. The high-concentration material can obtain better fluidity at higher temperature, and the problem of blockage caused by the increase of the material concentration is effectively solved, so that the operation of the whole evaporation concentration process is more stable.

The temperature sensor 3113 and the pressure sensor are mainly used for measuring the steam pressure and the steam temperature in the vaporizing section 311, and when the temperature and the pressure of the secondary steam separated in the vaporizing section 311 are insufficient, the flow rate of the forced circulation pump 261 needs to be properly increased through the PLC controller, and the amount of the material entering the vaporizing centrifugal chamber 31 is increased, so that the temperature and the air pressure of the secondary steam are increased. Level sensor 314 is mainly used for measuring the volume of piling up the material in settling chamber 32 and the vaporization centrifugal chamber 31, generally speaking, the position of material should be less than the position of hot material import 3111 in the settling chamber 32, if the liquid level of material is too high, then there may be the material in the evaporation unit 1 to pile up, lead to the material can't in time discharge, need suitably improve ejection of compact circulating pump 3331's flow through the PLC controller this moment, and open regulation formula bleeder valve 3333, make the material of piling up in the settling chamber 32 in time discharge. If level sensor 314 senses that the liquid level is in too high level for a long time, then the staff need in time carry out the machine halt to evaporating unit 1 and overhaul, and the manual work is handled accumulational material to guarantee that whole evaporation system operates steadily safely.

It should be noted that, when the external temperature is low, the fluidity of the material itself becomes poor, and the material is easily blocked when entering the feeding effect evaporation unit 13, so the preheater 72 is provided to heat the material at normal temperature to a suitable temperature, and then enter the heater 2 in the feeding effect evaporation unit 13 for evaporation and concentration. The material in the settling chamber 32 of the discharge effect evaporation unit 11 may mix with the supernatant liquid during discharge, so that the final product cannot reach the desired concentration. Therefore, the cyclone 8 is arranged, and the concentrated material in the discharging effect evaporation unit 11 is further centrifugally concentrated by a centrifugal separation mode, so that the material concentration is further improved.

The embodiment of this specific implementation mode is the preferred embodiment of the present invention, not limit according to this the utility model discloses a protection scope, so: all equivalent changes made according to the structure, shape and principle of the utility model are covered within the protection scope of the utility model.

Claims (9)

1. The utility model provides an evaporative concentration system of production high solid content solution, includes a plurality of evaporation unit (1) that link to each other, still includes steam generation device (4), comdenstion water collection device (5), vacuum pump (6) and stoste charge pump (7) that are connected with a plurality of evaporation unit (1) that link to each other, singly evaporation unit (1) is including heater (2) and sedimentation separator (3), the lateral wall upper end of heater (2) is provided with steam inlet (21) that link to each other with steam generation device (4), the lateral wall lower extreme of heater (2) is provided with comdenstion water export (22) that link to each other with comdenstion water collection device (5), its characterized in that: the sedimentation separator (3) comprises a vaporizing centrifugal chamber (31) and a sedimentation chamber (32) positioned below the vaporizing centrifugal chamber (31), the side wall of the vaporizing centrifugal chamber (31) is provided with a hot material inlet (3111), the top end of the heater (2) is provided with a hot material outlet (23), a hot material pipeline (24) is communicated and arranged between the hot material inlet (3111) and the hot material outlet (23), a clear liquid outlet (321) is arranged at the upper end of the side wall of the settling chamber (32), a clear liquid inlet (25) is arranged at the bottom end of the heater (2), a clear liquid pipeline (26) is arranged between the clear liquid outlet (321) and the clear liquid inlet (25), a forced circulation pump (261) is arranged on the clear liquid pipeline (26), a secondary steam outlet (3112) is arranged at the top end of the vaporizing centrifugal chamber (31), and a discharge hole (3332) is arranged at the bottom end of the settling chamber (32).

2. An evaporative concentration system for producing a high solids solution as set forth in claim 1 wherein: the vaporizing centrifugal chamber (31) comprises a vaporizing section (311) and a centrifugal section (312) which is connected and arranged at the lower end of the vaporizing section (311), a hot material inlet (3111) is arranged at the junction of the vaporizing section (311) and the centrifugal section (312), the feeding direction of the hot material inlet (3111) is coincided with the tangential direction of the radial section of the centrifugal section (312), and the tail end of the centrifugal section (312) is inserted into a settling chamber (32) and the inner diameter of the centrifugal section (312) is uniformly reduced from top to bottom.

3. An evaporative concentration system for producing a high solids solution as set forth in claim 2 wherein: the inner wall of settling chamber (32) is provided with a plurality of stationary flow ring board (322), and is a plurality of stationary flow ring board (322) are arranged along the direction of height of settling chamber (32) and are set up, stationary flow ring board (322) are close to between the border of centrifugation section (312) and the outer wall of centrifugation section (312) and reserve the circulation clearance, clear liquid export (321) are located the top of the most upper end stationary flow ring board (322).

4. An evaporative concentration system for producing a high solids solution as set forth in claim 3 wherein: the top end of the vaporizing centrifugal chamber (31) is provided with a wire mesh demister (313).

5. An evaporative concentration system for producing a high solids solution as set forth in claim 4 wherein: the bottom of settling chamber (32) is provided with concentrate and collects section (33), concentrate export (331) and concentrate backward flow mouth (332) have been seted up on concentrate collection section (33) respectively, the intercommunication is provided with concentrate pipeline (333) between concentrate export (331) and concentrate backward flow mouth (332), be provided with ejection of compact circulating pump (3331) on concentrate pipeline (333), discharge gate (3332) set up between ejection of compact circulating pump (3331) and concentrate backward flow mouth (332), discharge gate (3332) department is provided with regulation formula bleeder valve (3333).

6. An evaporative concentration system for producing a high solids solution as set forth in claim 5 wherein: the top of vaporization section (311) is provided with temperature sensor (3113) and pressure sensor (3114), the juncture of vaporization section (311) and centrifugation section (312) is provided with level sensor (314), temperature sensor (3113), pressure sensor and level sensor (314) all are electrically connected with the PLC controller, the PLC controller is all electrically connected with force circulation pump (261), ejection of compact circulating pump (3331) and regulation formula bleeder valve (3333) in each evaporation unit (1).

7. An evaporative concentration system for producing a high solids solution as set forth in claim 6 wherein: the evaporation unit (1) directly connected with the steam generating device (4) through a steam inlet (21) of the heater (2) is a discharging effect evaporation unit (11), the evaporation unit (1) directly connected with a raw liquid feed pump (7) through a hot material inlet (3111) of the sedimentation separator (3) is a feeding effect evaporation unit (13), the rest evaporation units (1) are intermediate effect evaporation units (12), the steam inlets (21) of the heaters (2) in the intermediate effect evaporation units (12) and the feeding effect evaporation units (13) are connected with a secondary steam outlet (3112) of the previous effect evaporation unit (1), material supplementing ports (262) are arranged on clear liquid pipelines (26) in the intermediate effect evaporation units (12) and the discharging effect evaporation units (11), and the material supplementing ports (262) are arranged between the forced circulation pump (261) and the clear liquid outlet (321), each material supplementing opening (262) is connected with a material outlet (3332) of the next-effect evaporation unit (1).

8. An evaporative concentration system for producing a high solids solution as set forth in claim 7 wherein: the feed system is characterized in that a stock solution feeding pipe (71) is communicated between a stock solution feeding pump (7) and a hot material inlet (3111) of the feed effect evaporation unit (13), a preheater (72) is connected to the stock solution feeding pipe (71), and the preheater (72) is connected with a secondary steam outlet (3112) in the feed effect evaporation unit (13).

9. An evaporative concentration system for producing a high solids solution as set forth in claim 8 wherein: still be provided with swirler (8) on concentrated material pipeline (333) in the evaporation unit is imitated in the play material (11), swirler (8) are including tangential feed inlet (81) and overflow mouth (82), between concentrated material backward flow mouth (332) and ejection of compact circulating pump (3331) in evaporation unit (11) are imitated in the ejection of compact to swirler (8) setting, be connected through concentrated material pipeline (333) between overflow mouth (82) and the concentrated feed back mouth, connect through concentrated material pipeline (333) between tangential feed inlet (81) and ejection of compact circulating pump (3331), discharge gate (3332) of evaporation unit (11) are imitated in the play material sets up the bottom in swirler (8).

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