CN111569462A - Continuous evaporation concentration crystallization device - Google Patents
Continuous evaporation concentration crystallization device Download PDFInfo
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- CN111569462A CN111569462A CN202010639646.XA CN202010639646A CN111569462A CN 111569462 A CN111569462 A CN 111569462A CN 202010639646 A CN202010639646 A CN 202010639646A CN 111569462 A CN111569462 A CN 111569462A
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 30
- 230000008025 crystallization Effects 0.000 title claims abstract description 30
- 230000008020 evaporation Effects 0.000 title abstract description 13
- 238000001704 evaporation Methods 0.000 title abstract description 13
- 239000000463 material Substances 0.000 claims abstract description 54
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims description 28
- 230000008569 process Effects 0.000 claims description 21
- 238000004458 analytical method Methods 0.000 claims description 8
- 230000000712 assembly Effects 0.000 claims description 6
- 238000000429 assembly Methods 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims 1
- 238000012546 transfer Methods 0.000 description 6
- 239000000543 intermediate Substances 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000011552 falling film Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 238000004886 process control Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 238000004506 ultrasonic cleaning Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
- B01D9/0031—Evaporation of components of the mixture to be separated by heating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0004—Crystallisation cooling by heat exchange
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- Crystallography & Structural Chemistry (AREA)
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Abstract
The invention discloses a continuous evaporation concentration crystallization device, comprising: the input end of the reaction module inputs materials, and the output end of the reaction module outputs heated materials; the piston device is connected with the reaction module in parallel, one end of the piston device is communicated with the input end of the reaction module, and the other end of the piston device is communicated with the output end of the piston device and used for providing piston push-pull power to enable the materials to flow and fully exchange heat; the heat exchange module is arranged in the reaction module and used for adjusting the reaction temperature in the reaction module; and the input end of the gas-liquid separation module is connected with the output end of the reaction module and is used for carrying out gas-liquid separation on the heated material output by the reaction module. The invention has simple structure, effectively reduced heat exchange area, high heat exchange coefficient and high treatment efficiency, and ensures the miniaturization of the device; meanwhile, the heat exchange structure is not easy to scale, the evaporation treatment performance is more stable and durable, and the device is easy to control, reliable and easy to maintain.
Description
Technical Field
The invention relates to the technical field of evaporation concentration crystallization, in particular to a continuous evaporation concentration crystallization device.
Background
At present, the traditional evaporation concentration crystallization equipment is mainly prepared by falling film evaporation and forced circulation evaporation, is limited by the heat exchange coefficient of an evaporator and the selection of an evaporation process, and has a huge structure and cannot be miniaturized; the traditional evaporator is easy to scale, so that the heat exchange coefficient is reduced, and the evaporator cannot stably run for a long time according to the designed performance.
In general, the main drawbacks of conventional evaporators are as follows:
1. limited by the balance of evaporation process selection and heat transfer coefficient. The heat transfer area is generally great when the evaporimeter is designed according to the material characteristic to lead to the evaporimeter bulky.
2. For specific materials, the evaporator is easy to scale during operation, so that the heat exchange coefficient is continuously reduced, and the evaporator can not stably operate for a long time under the condition of maintaining the designed performance. The traditional solution is that the equipment is complicated and the cost rises because of additionally installing an ultrasonic cleaning system.
3. The traditional evaporator needs manual disassembly type cleaning in the cleaning process, so that the production investment and the operation cost are high.
Disclosure of Invention
According to an embodiment of the present invention, there is provided a continuous evaporative concentration crystallization apparatus, including:
the input end of the reaction module inputs materials, and the output end of the reaction module outputs the heated materials;
the piston device is connected with the reaction module in parallel, one end of the piston device is communicated with the input end of the reaction module, and the other end of the piston device is communicated with the output end of the piston device and used for providing piston push-pull power to enable the materials to flow and fully exchange heat;
the heat exchange module is arranged in the reaction module and used for adjusting the reaction temperature in the reaction module;
and the input end of the gas-liquid separation module is connected with the output end of the reaction module and is used for carrying out gas-liquid separation on the heated material output by the reaction module.
Further, the reaction module comprises: the input end of the first reaction tube in series is used for inputting materials and is communicated with one end of the piston device, and the output end of the last reaction tube in series is used for outputting a product after reaction and is communicated with the other end of the piston device.
Further, the reaction tube comprises:
a pipe body;
the reaction core body is fixedly arranged inside the tube body;
the material inlet is arranged on the pipe body and used for inputting materials;
the material outlet is arranged on the pipe body and used for outputting materials or outputting products after reaction;
the heat preservation layer wraps the outer surface of the pipe body.
Further, the reaction tube further comprises: the process analysis interface is arranged on the tube body and used for observing the reaction in the reaction tube and analyzing the process.
Further, the method also comprises the following steps: and the sensor is arranged on the process analysis interface and is used for acquiring reaction data and states in the reaction tube.
Further, the reaction core comprises:
the vibrating plates are arranged in parallel inside the pipe body and divide the inside of the pipe body into a plurality of sections along the radial direction of the pipe body;
the vibration plate fixing rods penetrate through and fix the vibration plates along the radial direction of the pipe body;
and the pair of tube plates are respectively arranged at two ends of the tube body.
Further, the heat exchange module comprises: the heat exchange module that a plurality of is whole or partial to be connected in series, every heat exchange module sets up in the reaction tube, and the heat exchange module is used for circulating heat transfer medium, and the series direction of heat exchange module is the same with the series direction of reaction tube.
Further, the heat exchange module includes:
the heat exchange tubes penetrate through the vibration plates along the radial direction of the tube body, and two ends of each heat exchange tube penetrate through the tube plates respectively;
and the pair of end enclosure assemblies are respectively connected to the outer sides of the pair of tube plates and are respectively communicated with two ends of each heat exchange tube.
Further, the head subassembly contains: the heat exchange tube comprises a seal head and a seal head connecting tube, wherein the seal head is used for communicating the heat exchange tube, and the seal head connecting tube is used for inputting or outputting a heat exchange medium.
Further, every vibrates the board and all is equipped with a plurality of through-holes, and a plurality of through-holes are used for wearing to establish respectively and vibrate board dead lever and heat exchange tube to and be used for the material circulation.
Further, the method also comprises the following steps: and the material to be processed enters the second reaction module from the input end of the second reaction module, and is input into the input end of the reaction module from the output end of the second reaction module after reaction.
Further, the method also comprises the following steps: and the heat exchange medium flows into the second heat exchange module after flowing out of the heat exchange module and then flows out of the output end of the second heat exchange module.
Furthermore, the input end of the gas-liquid separation module is connected with the output end of the reaction module, the steam output end of the gas-liquid separation module is connected with the input end of the heat exchange module, the intermediate state output end of the gas-liquid separation module is connected with the input end of the reaction module, and the output end of the gas-liquid separation module outputs materials reaching the concentrated specified concentration.
The continuous evaporative concentration crystallization device provided by the embodiment of the invention has the advantages that the structure is simple, the heat exchange area is effectively reduced, the miniaturization of the device is ensured, the heat exchange coefficient is high, and the treatment efficiency is high; meanwhile, the heat exchange structure is not easy to scale, the evaporation treatment performance is more stable and durable, and the device is easy to control, reliable and easy to maintain.
It is to be understood that both the foregoing general description and the following detailed description are exemplary and are intended to provide further explanation of the claimed technology.
Drawings
FIG. 1 is a schematic structural diagram of a continuous evaporative concentration crystallization device according to an embodiment of the present invention;
FIG. 2 is a schematic structural view of the reaction module and the heat exchange module in FIG. 1;
FIG. 3 is a schematic view of the housing of FIG. 2;
FIG. 4 is an internal schematic view of FIG. 2;
FIG. 5 is a schematic view of the vibrating plate of FIG. 1;
FIG. 6 is a schematic view showing the material flow pattern of a continuous evaporative concentration crystallization apparatus according to an embodiment of the present invention;
FIG. 7 is a schematic structural diagram of a continuous evaporative concentration crystallization device provided with a second reaction module and a second heat exchange module according to an embodiment of the present invention.
Detailed Description
The present invention will be further explained by describing preferred embodiments of the present invention in detail with reference to the accompanying drawings.
First, a continuous evaporative concentration crystallization device according to an embodiment of the present invention will be described with reference to fig. 1 to 7, which is used in the field of evaporative concentration crystallization of materials and has a wide application range.
As shown in fig. 1, the continuous evaporative concentration crystallization apparatus according to the embodiment of the present invention includes a reaction module 1, a piston device 2, a heat exchange module 3, and a gas-liquid separation module 4.
Specifically, as shown in fig. 1, the input end of the reaction module 1 inputs materials, and the output end of the reaction module 1 outputs reacted products, and the reaction module has: the input end of the first reaction tube 11 connected in series inputs materials and is communicated with one end of the piston device 2, and the output end of the last reaction tube 11 connected in series outputs reacted products and is communicated with the other end of the piston device 2.
Further, as shown in FIGS. 2 to 4, the reaction tube 11 includes: the reactor comprises a tube body 111, a reaction core body 112, a material inlet 113, a material outlet 114 and an insulating layer 115, wherein the reaction core body 112 is fixedly arranged inside the tube body 111; the material inlet 113 is arranged on the tube body 111 and used for inputting materials; the material outlet 114 is arranged on the tube body 111 and is used for outputting materials or outputting products after reaction; the insulating layer 115 is wrapped around the outer surface of the pipe body 111.
Further, as shown in fig. 1 to 3, the reaction tube 11 further includes: a process analysis interface 116, wherein the process analysis interface 116 is disposed on the tube body 111 for observing the reaction in the reaction tube 11 and analyzing the process. In this embodiment, the continuous plug flow vortex flow reactor of the embodiment of the present invention further has a sensor 5, the sensor 5 is disposed on the process analysis interface 116, and uses a process analysis technique to collect the reaction data and status in the reaction tube 11, such as: the data of raw materials, intermediates and final products are convenient for understanding the influence mode of process variables on systems based on physics, chemistry and biology, provide opportunities for the detection of unknown intermediates, mechanisms and end points, and can be adopted in the processes of research and development, amplified production and process control.
Further, as shown in fig. 2 and 4, the reaction core 112 includes: a plurality of vibration plates 1121, a plurality of vibration plate fixing rods 1122, and a pair of tube plates 1123. The oscillating plates 1121 are arranged inside the tube 111 in parallel, and the oscillating plates 1121 divide the inside of the tube 111 into a plurality of sections along the radial direction of the tube 111, so that a plurality of small reaction kettles connected in series are formed among the oscillating plates 1121; each vibration plate fixing rod 1122 penetrates through and fixes a plurality of vibration plates 1121 along the radial direction of the pipe body 111; a pair of tube sheets 1123 are provided at both ends of the tube body 111, respectively.
Specifically, as shown in fig. 1, the piston device 2 is connected in parallel with the reaction module 1, one end of the piston device 2 is communicated with the input end of the reaction module 1, and the other end of the piston device 2 is communicated with the output end of the piston device 2, so as to provide a piston push-pull power to make the materials flow and be fully mixed.
Specifically, as shown in fig. 1, 2 and 4, the heat exchange module 3 is disposed in the reaction module 1, and is used for adjusting the reaction temperature in the reaction module 1, and has: a plurality of heat exchange module 31 wholly or partly establish ties, every heat exchange module 31 sets up in reaction tube 11, and heat exchange module 31 is used for circulating heat transfer medium, and heat exchange module 31's series direction is the same with reaction tube 11's series direction, further makes compact, simple reliable easy the maintenance. In this embodiment, when all the heat exchange modules 31 are connected in series, the same heat exchange medium is used; when a plurality of heat exchange module 31 parts are connected in series, the parts connected in series adopt the same heat exchange medium, and adopt different heat exchange media as required, so as to achieve better heat exchange effect.
Further, as shown in fig. 1, 2 and 4, the heat exchange module 31 includes: a plurality of heat exchange tubes 311 and a pair of end enclosure assemblies 312.
Wherein, as shown in fig. 1, 2, and 4, the plurality of heat exchange tubes 311 radially pass through the plurality of oscillating plates 1121 along the tube body 111, and both ends of each heat exchange tube 311 respectively pass through the pair of tube sheets 1123, so that, due to the division of the heat exchange tubes 311, a plurality of small parallel reaction kettles are formed between any two oscillating plates 1121, and a plurality of small serial reaction kettles are formed between the plurality of oscillating plates 1121, in addition to the active mixing of the piston device 2, as shown in fig. 6, so that the material fluid fully reacts in the form of piston flow and vortex flow at the reaction core 112, the piston flow mass transfer effect is equivalent to the serial connection of a plurality of continuous kettle-type reactors, the mixing frequency and the mass transfer rate are both higher than 1-2 orders of magnitude of the large kettle-type reactor, the fluid dispersion coefficient is small, the residence time is wide 10s-10h, and the forward flow reaction and the reverse flow reaction can be performed, therefore, the process time is greatly shortened, the efficiency is higher, and the control is easy.
As shown in fig. 1, 2 and 4, a pair of head assemblies 312 are respectively connected to the outer sides of the pair of tube sheets 1123, and the pair of head assemblies 312 are respectively communicated with both ends of each heat exchange tube 311, in this embodiment, the head assemblies 312 have: the heat exchange tube 3121 is connected with the end socket 3121, the end socket 3121 is used for connecting with the heat exchange tube 311, and the end socket 3122 is used for inputting or outputting heat exchange medium. The material flows in the form of piston flow and vortex flow at the reaction core 112 to effectively improve the heat exchange coefficient between the material and the heat exchange medium in the heat exchange tube 311, the effect is equivalent to more than 3 times of laminar heat exchange, thereby the heating area of the heat exchange module 3 meets the heat exchange requirement under the condition of smaller heating area, and the material can effectively remove the attached dirt on the heat exchange tube 311 under the form of piston flow and vortex flow, the shutdown maintenance cost of the equipment is reduced, the shutdown cleaning maintenance can realize online cleaning without disassembly, and the heat exchange performance is ensured to be kept stable.
Further, as shown in fig. 5, each vibration plate 1121 is provided with a plurality of through holes 11211, and the plurality of through holes 11211 are respectively used for penetrating through the vibration plate fixing rod 1122 and the heat exchange tube 311 and for material circulation.
Specifically, the input end 41 of the gas-liquid separation module 4 is connected to the output end 114 of the reaction module 1, and is configured to perform gas-liquid separation on the concentrated material output by the reaction module 1, in this embodiment, as shown in fig. 1 and 7, the gas-liquid separation module 4 is selected from a gas-liquid separator, the gas-liquid separator is further provided with a steam output end 42 and an output end 43, and if necessary, the gas-liquid separator is further provided with an intermediate state output end 44 for a cyclic reaction.
When the reactor works, as shown in fig. 1, a material enters a cavity formed by the tube body 111, the tube plate 1123, the oscillating plate 1121, the oscillating plate rod 1122 and the heat exchange tube 311 from the material inlet 113, and reciprocates at a through hole on the oscillating plate 1121 in the cavity, so that processes of mixing, heat exchange, reaction, crystallization and the like are completed, and the mixture is discharged to the gas-liquid separation module 4 through the material outlet 114, wherein a heat exchange medium enters the heat exchange tube 311 through the end enclosure 3121 and the end enclosure connecting tube 3122, and flows out through the end enclosure 3121 at the other end of the reaction core 112 and the end enclosure connecting tube 3122, so that the heat exchange process is completed. The reacted materials are gasified in the gas-liquid separation module 4 to generate steam, the part left in the gas-liquid separation module 4 is concentrated and crystallized, and the steam is output by the output end of the gas-liquid separation module 4 after reaching the corresponding concentration.
Further, as shown in fig. 7, the continuous evaporative concentration crystallization apparatus according to the embodiment of the present invention further includes: a second reaction module 6 and a second heat exchange module 7.
Specifically, as shown in fig. 7, the second reaction module 6 is connected in series with the reaction module 1, and the material to be processed enters the second reaction module 6 from the input end of the second reaction module 6, and is input into the input end of the reaction module 1 from the output end of the second reaction module 6 after reaction.
Specifically, as shown in fig. 7, the second heat exchange module 7 is disposed in the second reaction module 6, an input end of the second heat exchange module 7 is connected to an output end of the heat exchange module 3, and the heat exchange medium flows out of the heat exchange module 3, flows into the second heat exchange module 7, and flows out of an output end of the second heat exchange module 7.
Further, as shown in fig. 7, the second reaction module 6 has the same structure as the reaction module 1, and the second heat exchange module 7 has the same structure as the heat exchange module 3, in this embodiment, the second reaction module 6 is provided with a second reaction tube 61 having the same structure as the reaction tube 11.
Further, due to the fact that the second heat exchange module 7 and the second reaction module 6 are adopted, the input end of the gas-liquid separation module 4 is connected with the output end of the reaction module 1, the steam output end of the gas-liquid separation module 4 is connected with the input end of the heat exchange module 3, the intermediate state output end of the gas-liquid separation module 4 is connected with the input end of the reaction module 1, and the output end of the gas-liquid separation module 4 outputs materials reaching the concentrated designated concentration.
When the reactor works, materials are input from the input end of the second reaction module 6, and then enter the gas-liquid separation module 4 through the reaction module 1, and the specific reaction and gas-liquid separation processes are the same as the principle, and are not described again here. The difference lies in that the heat exchange medium in the heat exchange module 3 and the second heat exchange module 7 adopts the high-temperature steam generated in the gas-liquid separation module 4, thereby not only finishing heat exchange, realizing the recycling of energy sources and greatly improving economic benefits, but also realizing the modularized assembly of the whole equipment and having simple structure and easy control.
In the above, with reference to fig. 1 to 7, the continuous evaporative concentration crystallization device according to the embodiment of the present invention is described, which has a simple structure, effectively reduces the heat exchange area, ensures miniaturization of the device, and has a high heat exchange coefficient and a high treatment efficiency; meanwhile, the heat exchange structure is not easy to scale, the evaporation treatment performance is more stable and durable, and the device is easy to control, reliable and easy to maintain.
It should be noted that, in the present specification, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
While the present invention has been described in detail with reference to the preferred embodiments, it should be understood that the above description should not be taken as limiting the invention. Various modifications and alterations to this invention will become apparent to those skilled in the art upon reading the foregoing description. Accordingly, the scope of the invention should be determined from the following claims.
Claims (13)
1. A continuous evaporative concentration crystallization device, comprising:
the input end of the reaction module inputs materials, and the output end of the reaction module outputs the heated materials;
the piston device is connected with the reaction module in parallel, one end of the piston device is communicated with the input end of the reaction module, and the other end of the piston device is communicated with the output end of the piston device and used for providing piston push-pull power to enable the materials to flow and fully exchange heat;
the heat exchange module is arranged in the reaction module and used for adjusting the reaction temperature in the reaction module;
and the input end of the gas-liquid separation module is connected with the output end of the reaction module and is used for carrying out gas-liquid separation on the heated material output by the reaction module.
2. The continuous evaporative concentration crystallization device of claim 1, wherein the reaction module comprises: the input end of the first reaction tube in series is used for inputting materials and is communicated with one end of the piston device, and the output end of the last reaction tube in series is used for outputting a reacted product and is communicated with the other end of the piston device.
3. The continuous evaporative concentration crystallization apparatus as set forth in claim 2, wherein the reaction tube comprises:
a pipe body;
the reaction core body is fixedly arranged inside the tube body;
the material inlet is arranged on the pipe body and used for inputting materials;
the material outlet is arranged on the pipe body and used for outputting materials or outputting a product after reaction;
and the heat insulation layer is wrapped on the outer surface of the pipe body.
4. The continuous evaporative concentration crystallization apparatus as set forth in claim 3, wherein the reaction tube further comprises: and the process analysis interface is arranged on the tube body and used for observing and analyzing the reaction in the reaction tube.
5. The continuous evaporative concentration crystallization apparatus as set forth in claim 4, further comprising: and the sensor is arranged on the process analysis interface and is used for acquiring reaction data and states in the reaction tube.
6. The continuous evaporative concentration crystallization apparatus as claimed in claim 3 or 4, wherein the reaction core comprises:
the vibration plates are arranged in parallel inside the pipe body and divide the inside of the pipe body into a plurality of sections along the radial direction of the pipe body;
the vibration plate fixing rods penetrate through and fix the vibration plates along the radial direction of the pipe body;
and the pair of tube plates are respectively arranged at two ends of the tube body.
7. The continuous evaporative concentration crystallization device as claimed in claim 6, wherein the heat exchange module comprises: the heat exchange device comprises a plurality of heat exchange modules which are wholly or partially connected in series, wherein each heat exchange module is arranged in a reaction tube and used for circulating a heat exchange medium, and the serial direction of the heat exchange modules is the same as that of the reaction tubes.
8. The continuous evaporative concentration crystallization device as claimed in claim 7, wherein the heat exchange module comprises:
the heat exchange tubes penetrate through the oscillating plates along the radial direction of the tube body, and two ends of each heat exchange tube penetrate through the pair of tube plates respectively;
and the pair of end enclosure assemblies are respectively connected to the outer sides of the pair of tube plates and are respectively communicated with two ends of each heat exchange tube.
9. The continuous evaporative concentration crystallization device as claimed in claim 8, wherein the head assembly comprises: the heat exchange tube comprises a head and a head connecting tube, wherein the head is used for communicating the heat exchange tube, and the head connecting tube is used for inputting or outputting a heat exchange medium.
10. The continuous evaporative concentration crystallization device as claimed in claim 8, wherein each of the oscillating plates is provided with a plurality of through holes for respectively passing through the oscillating plate fixing rod and the heat exchange tube and for material circulation.
11. The continuous evaporative concentration crystallization apparatus as set forth in claim 1 or 8, further comprising: the second reaction module is connected with the reaction module in series, and the material to be treated enters the second reaction module from the input end of the second reaction module and is input to the input end of the reaction module from the output end of the second reaction module after reaction.
12. The continuous evaporative concentration crystallization apparatus as set forth in claim 11, further comprising: and the second heat exchange module is arranged in the second reaction module, the input end of the second heat exchange module is connected with the output end of the heat exchange module, and a heat exchange medium flows into the second heat exchange module after flowing out of the heat exchange module and then flows out of the output end of the second heat exchange module.
13. The continuous evaporative concentration crystallization device as claimed in claim 12, wherein the input end of the gas-liquid separation module is connected to the output end of the reaction module, the steam output end of the gas-liquid separation module is connected to the input end of the heat exchange module, the intermediate output end of the gas-liquid separation module is connected to the input end of the reaction module, and the output end of the gas-liquid separation module outputs the material reaching the concentration specified concentration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010639646.XA CN111569462B (en) | 2020-07-06 | 2020-07-06 | Continuous evaporating, concentrating and crystallizing device |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202010639646.XA CN111569462B (en) | 2020-07-06 | 2020-07-06 | Continuous evaporating, concentrating and crystallizing device |
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| CN111569462A true CN111569462A (en) | 2020-08-25 |
| CN111569462B CN111569462B (en) | 2024-07-02 |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111760544A (en) * | 2020-07-06 | 2020-10-13 | 上海济俭工业设备有限公司 | Continuous plug flow eddy current reaction device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104524798A (en) * | 2015-01-18 | 2015-04-22 | 丁武轩 | Continuous evaporation and crystallization device and method capable of saving energy by mechanical steam recompression |
| CN104548652A (en) * | 2015-01-25 | 2015-04-29 | 陈式好 | Continuous evaporative crystallization system |
| CN212881134U (en) * | 2020-07-06 | 2021-04-06 | 上海济俭工业设备有限公司 | Continuous evaporation concentration crystallization device |
-
2020
- 2020-07-06 CN CN202010639646.XA patent/CN111569462B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104524798A (en) * | 2015-01-18 | 2015-04-22 | 丁武轩 | Continuous evaporation and crystallization device and method capable of saving energy by mechanical steam recompression |
| CN104548652A (en) * | 2015-01-25 | 2015-04-29 | 陈式好 | Continuous evaporative crystallization system |
| CN212881134U (en) * | 2020-07-06 | 2021-04-06 | 上海济俭工业设备有限公司 | Continuous evaporation concentration crystallization device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111760544A (en) * | 2020-07-06 | 2020-10-13 | 上海济俭工业设备有限公司 | Continuous plug flow eddy current reaction device |
| CN111760544B (en) * | 2020-07-06 | 2023-07-25 | 上海济俭工业设备有限公司 | Continuous plug flow swirling flow reaction device |
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| Publication number | Publication date |
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| CN111569462B (en) | 2024-07-02 |
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