CN107854857B - Multi-pass concentration and purification device and using method thereof - Google Patents

Multi-pass concentration and purification device and using method thereof Download PDF

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CN107854857B
CN107854857B CN201711413470.0A CN201711413470A CN107854857B CN 107854857 B CN107854857 B CN 107854857B CN 201711413470 A CN201711413470 A CN 201711413470A CN 107854857 B CN107854857 B CN 107854857B
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chamber
steaming
steaming chamber
evaporation
liquid
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CN107854857A (en
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王启阳
王进坚
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Wuxi Chengerxin Environmental Protection Equipment Technology Co ltd
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Wuxi Chengerxin Environmental Protection Equipment Technology Co ltd
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    • BPERFORMING OPERATIONS; TRANSPORTING
    • B01PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01DSEPARATION
    • B01D1/00Evaporating
    • B01D1/26Multiple-effect evaporating

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Abstract

The invention relates to the technical field of liquid concentration and purification, in particular to a multi-pass concentration and purification device and a using method thereof. This concentrated purification device of journey, rational in infrastructure, low cost, low energy consumption, low row improve industrial production and pollution control trade clean production level, and the reduction pollutant produces, reduces the energy consumption, practices thrift the running cost, saves the heating energy resource consumption, and waste heat utilization rate is high, and the secondary steam utilization ratio reaches more than 95% to compromise the gas-liquid exchange that the evaporation spilled over gas, two functions of waste heat utilization and gas-liquid exchange realize in step. The vacuum negative pressure circulation evaporation has the advantages of low evaporation temperature, high evaporation efficiency, good adaptability of heating energy, low energy consumption, even heating by utilizing a waste heat source, energy conservation and emission reduction.

Description

Multi-pass concentration and purification device and using method thereof
Technical Field
The invention relates to the technical field of liquid concentration and purification, in particular to a multi-pass concentration and purification device and a using method thereof.
Background
An intelligent multi-pass digester is a device for concentrating and purifying liquid under vacuum condition. The device is suitable for concentrating and purifying relevant liquid in the industries of chemical industry, metallurgy, nonferrous metals, surface treatment, textile dyeing and finishing, medicine, food, papermaking, seawater desalination and the like, is also suitable for recycling waste and harmless recycling, reduces waste discharge, improves the resource utilization rate, and is production, pollution treatment and waste recycling equipment with wide application in the industries of industrial production, environmental treatment and the like. The application of the invention can save the production and pollution treatment cost, reduce the energy consumption, save the water resource, efficiently utilize the waste resource, reduce the waste emission, has no secondary pollution, and has the advantages of wide application field, good applicability, high intelligent degree, energy conservation and emission reduction and obviously improved economic benefit.
The invention aims to provide a multi-pass concentration and purification device which is reasonable in structure, low in cost, energy consumption and emission, improves the clean production level of industrial production and pollution control industries, reduces pollutants, reduces energy consumption and saves operation cost.
The invention relates to a multi-pass concentration and purification device, which has the following advantages:
1. the energy consumption of heating is saved, the utilization rate of waste heat is high, the utilization rate of secondary steam reaches more than 95%, the gas-liquid exchange of evaporation overflow gas is considered, and the two functions of waste heat utilization and gas-liquid exchange are synchronously realized.
2. The vacuum negative pressure circulation evaporation has the advantages of low evaporation temperature, high evaporation efficiency, good adaptability of heating energy, low energy consumption, even heating by utilizing a waste heat source, energy conservation and emission reduction.
3. High concentration and purification yield and stable product quality.
4. The material causticization harm is small, the scaling and fouling are less, the service life is long, and the maintenance period is long.
5. The system has the advantages of few faults, good safety performance, stable operation, simple and convenient operation, and compatibility with remote control, and can realize the operation of man-machine separation control.
6. The electric energy consumption is saved, and the circulating evaporation is mainly completed by vacuum self-absorption diversion.
7. The utilization rate of water resources is high, the PH value of condensed water generated by evaporation of the non-volatile liquid is between 7.2 and 7.5, and the condensed water can be completely used for production and recycling, the temperature of the condensed water is between 75 and 85 ℃, and the heating energy consumption in recycling is saved.
8. The environment-friendly effect is good, the waste and sewage discharge is less, the generated waste recycling rate and collection rate are high, the cyclic utilization rate is high, and the resource consumption is reduced.
9. The intelligent degree is high, and the operation and safety guarantee of each system realize the full coverage of the intelligent technology.
10. Wide industrial application field and great applicability to liquid concentration and purification.
Disclosure of Invention
In order to overcome the defects in the background art, the technical scheme adopted by the invention for solving the technical problems is as follows: a multi-pass concentration and purification device comprises a preheating type solid-liquid separator, a multi-pass steaming chamber, a thickening circulating pump, a filter and a raw liquid storage tank, wherein a raw liquid conveying pump is arranged between the filter and the raw liquid storage tank, the preheating type solid-liquid separator and the filter are connected together through a pipeline, the raw liquid storage tank and the impurity collection tank are connected together through a pipeline, the preheating type solid-liquid separator is connected with the circulating pump and an inner pipe of a heat exchanger in series, a pre-thickening circulating pump is arranged on a pipeline between the preheating type solid-liquid separator and an inner pipe of an external heater, the multi-pass steaming chamber comprises a first steaming chamber, a second steaming chamber, a third steaming chamber, a fourth steaming chamber, a fifth steaming chamber, a sixth steaming chamber, a seventh steaming chamber, an eighth steaming chamber, a ninth steaming chamber and a tenth chamber, the first steaming chamber, the second steaming chamber, the third steaming chamber, the fourth steaming chamber, the fifth chamber, the seventh steaming chamber, the eighth steaming chamber, the ninth chamber and the tenth chamber, the condensate water collecting tank is connected with a water collecting tank through a water collecting tank, and a water collecting tank are connected with the upper portion of the vapor-liquid collecting tank; the steam refining chamber I, the steam refining chamber II, the steam refining chamber III, the steam refining chamber IV, the steam refining chamber V, the steam refining chamber VI, the steam refining chamber VII, the steam refining chamber VIII and the steam refining chamber IX are arranged in the vaporization separation chamber, the steam refining chamber IX is arranged at the bottom of the steam refining chamber IV through a pipeline and is connected together with the steam refining chamber VI, the steam refining chamber IX is arranged at the bottom of the steam refining chamber IV through a pipeline and is connected together, the steam refining chamber IX is arranged at the bottom of the steam refining chamber II through a pipeline and is connected together with the steam refining chamber IV, the steam refining chamber IV is connected together with the steam refining chamber III through a pipeline and is connected together with the steam refining chamber IV, the steam refining chamber III is connected together through a vacuum valve and a vacuum connecting pipe, the steam refining chamber IV is connected together with the steam refining chamber IV and is connected together through a vacuum connecting pipe, the steam refining chamber IV and a vacuum connecting pipe, the top parts of the four steaming chambers and the three steaming chambers are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve, the top parts of the three steaming chambers and the two steaming chambers are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve, the top parts of the two steaming chambers and the first steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve, a connecting pipeline between a pre-concentration circulating pump and an inner pipe of an external heater passes through a gas-liquid exchange chamber of the five steaming chambers, the four steaming chambers, the three steaming chambers, the two steaming chambers and the first steaming chamber, a steam inlet pipe passes through an interlayer of the external heater and then enters a self-cleaning exhaust gas evaporator, the bottom part of the eight steaming chambers and a gas-barrier settler are connected together through pipelines, a circulating balance pump is arranged on a connecting pipeline between the non-exhaust gas evaporator and the gas-barrier settler and the first sundries collecting tank, a condensate water tank of the eight steaming chambers and a condensate water collecting tank of the nine steaming chambers are connected together through a condensate water collecting tank of the nine steaming chambers and a condensate water collecting tank of the nine steaming chambers, the nine steaming chambers and a condensate water collecting tank of the eight steaming chambers are connected together through a condensate water collecting tank and a condensate water tank of the nine steaming chambers, the concentrated liquid storage tank is communicated with the crystal and liquid separator and the concentrated liquid storage tank through pipelines provided with product delivery pumps, the crystal and liquid separator are connected with the crystal recovery tank through pipelines, the crystal and liquid separator are connected with the solid-liquid separator through pipelines provided with concentrated liquid output pumps, the crystal and liquid separator are connected with the crystal recovery tank through pipelines, the crystal and liquid separator are connected with the solid-liquid separator through pipelines, the vacuum pump is sequentially communicated with the condensate water recovery tank, the distillation chamber nine and the distillation chamber ten through interlayers of a vacuum generator and an erosion eliminator through pipelines, the cooling water tank is communicated with the cooling water tank through an inner pipe provided with a cooling pump through an air erosion eliminator, the cooling water tank is communicated with the cooling water tank through a pipeline provided with a distillation chamber cooling pump through an air-liquid exchange chamber of the distillation chamber eight, the distillation chamber nine and the distillation chamber ten through an interlayer of a heat exchanger, and a cooling tower is arranged outside the cooling water tank.
Preferably, a gas-liquid mixing pump is arranged outside the preheating type solid-liquid separator, the self-cleaning type exhaust gas evaporator and the solid-liquid separator.
Preferably, a refrigerator is arranged on the vacuum generator.
The using method of the multi-pass concentration and purification device comprises the following steps:
(1) Firstly, raw materials to be processed are collected in a stock solution storage tank, then the stock solution is conveyed into a filter by a stock solution conveying pump, the raw materials filtered by the filter enter a preheating type solid-liquid separator, and impurities filtered by the filter are conveyed into a sundries collecting box II;
(2) The heat source of the preheating type solid-liquid separator is from a gas-liquid exchange chamber of the eight cooking chamber, the nine cooking chamber and the ten cooking chamber, the cooling water tank passes through the gas-liquid exchange chambers of the eight cooking chamber, the nine cooking chamber and the ten cooking chamber through a pipeline provided with a cooling pump of the cooking chamber, then is communicated with the cooling water tank through an interlayer of a heat exchanger, the preheating type solid-liquid separator is connected with a circulating pump and an inner pipe of the heat exchanger in series, and thus, the material in the preheating type solid-liquid separator is heated through the heat exchanger;
(3) The circulating pump sends the materials in the preheating type solid-liquid separator into the pre-concentration circulating pump, and the pre-concentration circulating pump preliminarily heats the materials in a gas-liquid exchange chamber of a fifth steaming chamber, a fourth steaming chamber, a third steaming chamber, a second steaming chamber and a first steaming chamber, then the materials enter an external heater for further heating, and then the materials enter an evaporation bridge in the first steaming chamber;
(4) The vacuum pump is respectively communicated with the condensate water recovery tank, the steaming chamber nine and the steaming chamber ten through the vacuum generator and the interlayer of the gas erosion eliminator in sequence by pipelines, so that the condensate water recovery tank, the steaming chamber nine and the steaming chamber ten have the same vacuum degree; through the adjustment of an intelligent vacuum proportional valve, the vacuum degrees between a first distillation chamber, a second distillation chamber, a fifth distillation chamber, a fourth distillation chamber, a third distillation chamber, a second distillation chamber and a first distillation chamber are sequentially reduced, so under the action of negative pressure, materials sequentially enter the ninth distillation chamber from the first distillation chamber, the second distillation chamber, the third distillation chamber, the fourth distillation chamber, the fifth distillation chamber, the sixth distillation chamber, the seventh distillation chamber and the eighth distillation chamber through evaporation bridges, the materials in the ninth distillation chamber and the tenth distillation chamber are communicated with each other through series pipes, the solutions in the materials in the first distillation chamber, the second distillation chamber, the third distillation chamber, the fourth distillation chamber, the fifth distillation chamber, the sixth distillation chamber, the seventh distillation chamber, the eighth distillation chamber, the ninth distillation chamber and the tenth distillation chamber are evaporated into a gas-liquid exchange chamber at the upper part of a water collecting plate, and a liquid solution on the water collecting plate stays in a liquid-state water collecting plate, and a liquid solution can be recovered through a liquid-state water collecting tank;
(5) Then the materials form a preconcentration cycle through a preconcentration circulating pump, a first steaming chamber, a second steaming chamber, a third steaming chamber, a fourth steaming chamber, a fifth steaming chamber, a sixth steaming chamber, a seventh steaming chamber, an eighth steaming chamber, a choke settler, a circulation balance pump, a self-cleaning exhaust gas evaporator and the preconcentration circulating pump; the materials form an enrichment cycle through an enrichment circulating pump, a ninth steaming chamber and a tenth steaming chamber;
(6) After the material comes out through the thickening circulating pump, the crystal recycling box is recycled with the crystal to the entering crystal and the liquid separator that need the crystallization separation, and the back is come out through the thickening circulating pump to the material, and the incasement is kept in to the entering thick liquid that does not need the crystallization, and the concentrated material that the product delivery pump kept in the incasement with the thick liquid send people's solid-liquid separation ware, and the concentrated material that the thick liquid output pump was in with the solid-liquid separation ware sends people's thick liquid storage tank, accomplishes the concentrated purification of material.
The invention aims to provide a multi-pass concentration and purification device which is reasonable in structure, low in cost, energy consumption and emission, improves the clean production level of industrial production and pollution control industries, reduces pollutants, reduces energy consumption and saves operation cost.
The invention relates to a multi-pass concentration and purification device, which has the following advantages:
1. the waste heat utilization ratio is high, the utilization ratio of the secondary steam reaches more than 95 percent, the gas-liquid exchange of the evaporation overflow gas is considered, and the waste heat utilization function and the gas-liquid exchange function are synchronously realized.
2. The vacuum negative pressure circulation evaporation has the advantages of low evaporation temperature, high evaporation efficiency, good adaptability of heating energy, low energy consumption, even heating by utilizing a waste heat source, energy conservation and emission reduction.
3. High concentration and purification yield and stable product quality.
4. The material causticization harm is small, the scale and dirt deposition is less, the service life is long, and the maintenance period is long.
5. The system has the advantages of few faults, good safety performance, stable operation, simple and convenient operation, and compatibility with remote control, and can realize the operation of man-machine separation control.
6. The electric energy consumption is saved, and the circulating evaporation is mainly completed by vacuum self-absorption flow guide.
7. The utilization rate of water resources is high, the PH value of condensed water generated by evaporation of the non-volatile liquid is between 7.2 and 7.5, the condensed water can be completely used for production and recycling, the temperature of the condensed water is between 75 and 85 ℃, and the heating energy consumption in recycling is saved.
8. The environment-friendly effect is good, the waste and sewage discharge is less, the generated waste recycling rate and collection rate are high, the cyclic utilization rate is high, and the resource consumption is reduced.
9. The intelligent degree is high, and the operation and safety guarantee of each system realize the full coverage of the intelligent technology.
10. Wide industrial application field and great applicability to liquid concentration and purification.
Drawings
The invention is further illustrated with reference to the following figures and examples.
FIG. 1 is a schematic process flow diagram of a multi-pass concentration and purification apparatus according to the present invention;
FIG. 2 is a schematic view of the construction of a multi-pass distillation chamber according to the present invention;
wherein 1, a preheating type solid-liquid separator; 2. a multi-pass cooking chamber; 2-1, a first steaming chamber; 2-2, a second steaming chamber; 2-3, a third steaming chamber; 2-4, and a fourth steaming chamber; 2-5, a fifth distillation chamber; 2-6, and a sixth steaming chamber; 2-7, a seventh steaming chamber; 2-8, and eighthly, a steaming chamber; 2-9, a ninth steaming chamber; 2-10, ten steaming chambers; 3. a gas barrier settler; 4. a self-cleaning exhaust gas evaporator; 5. an external heater; 6. a cavitation eliminator; 7. a vacuum generator; 8. a condensed water collection and storage tank; 9. a stock solution delivery pump; 10. a pre-concentration circulating pump; 11. a thickening circulating pump; 12. a gas-liquid mixing pump; 13. a heat exchanger; 14. a filter; 15. a stock solution storage tank; 16. a cooling tower; 17. a refrigerator; 18. a vacuum pump; 19. a concentrated solution storage tank; 20. a concentrated liquid output pump; 21. a solid-liquid separator; 22. a crystal and liquid separator; 23. a crystal recovery box; 24. a concentrated solution temporary storage box; 25. a cooling water tank; 26. a steam inlet pipe; 27. a sundries collecting box I; 28. a second sundry collecting box; 29. a Roots air extractor; 30. a circulating balance pump; 31. a cooling pump of the distillation chamber; 32. a condensed water recovery tank; 33. a circulation pump; 34. water collecting plates; 35. an evaporation bridge; 36. a pipe is connected in series; 37. an intelligent vacuum proportional valve; 38. a product delivery pump; 39. and (4) cooling the pump.
Detailed Description
The present invention will now be described in further detail with reference to the accompanying drawings. The drawings are simplified schematic views illustrating only the basic structure of the present invention in a schematic manner, and thus show only the constitution related to the present invention.
In the embodiment, referring to fig. 1-2, a multi-pass concentrating and purifying apparatus includes a preheating solid-liquid separator 1, a multi-pass steaming chamber 2, a concentration circulating pump 11, a filter 14 and a stock solution storage tank 15, a stock solution delivery pump 9 is arranged between the filter 14 and the stock solution storage tank 15, the preheating type solid-liquid separator 1 and the filter 14 are connected together through a pipeline, the preheating solid-liquid separator 1 and the filter 14 are connected with the second sundries collecting box 28 through pipelines, the second sundries collecting box 28 is connected with the stock solution storage tank 15 through a pipeline, the preheating type solid-liquid separator 1 is connected with a circulating pump 33 and an inner pipe of the heat exchanger 13 in series, a pre-concentration circulating pump 10 is arranged on a pipeline between the preheating type solid-liquid separator 1 and the inner pipe of the external heater 5, the multi-pass steaming chamber 2 comprises a first steaming chamber 2-1, a second steaming chamber 2-2, a third steaming chamber 2-3, a fourth steaming chamber 2-4, a fifth steaming chamber 2-5, a sixth steaming chamber 2-6, a seventh steaming chamber 2-7, an eighth steaming chamber 2-8, a ninth steaming chamber 2-9 and a tenth steaming chamber 2-10, the middle parts of the first steaming chamber 2-1, the second steaming chamber 2-2, the third steaming chamber 2-3, the fourth steaming chamber 2-4, the fifth steaming chamber 2-5, the sixth steaming chamber 2-6, the seventh steaming chamber 2-7, the eighth steaming chamber 2-8, the ninth steaming chamber 2-9 and the tenth steaming chamber 2-10 are provided with a water collecting plate 34, the water collecting plate 34 is connected with a condensate water recovery tank 32 through a connecting pipeline, the upper part of the water collecting plate 34 is a gas-liquid exchange chamber, and the lower part of the water collecting plate 34 is a vaporization separation chamber; the evaporation device comprises a first evaporation chamber 2-1, a second evaporation chamber 2-2, a third evaporation chamber 2-3, a fourth evaporation chamber 2-4, a fifth evaporation chamber 2-5, a sixth evaporation chamber 2-6, a seventh evaporation chamber 2-7, an eighth evaporation chamber 2-8 and a ninth evaporation chamber 2-9, wherein evaporation bridges 35 are arranged in the vaporization separation chambers of the first evaporation chamber 2-4, the fifth evaporation chamber 2-5, the eighth evaporation chamber 2-8, the evaporation bridges 35 in the eighth evaporation chamber 2-8 and the seventh evaporation chamber 2-7, the evaporation bridges 35 in the seventh evaporation chamber 2-7 and the sixth evaporation chamber 2-6 are connected together through pipelines, the evaporation bridges 35 in the sixth evaporation chamber 2-6 and the fifth evaporation chamber 2-5 are connected together through pipelines, the evaporation bridges 35 in the fifth evaporation chamber 2-5 and the fourth evaporation chamber 2-4 are connected together through pipelines, the evaporation bridges 35 in the fifth evaporation chamber 2-5 and the fifth evaporation chamber 2-5 are connected together through a first evaporation chamber 2-4, the first evaporation chamber 2-4 and the ninth evaporation chamber 2-4 are connected together through a first evaporation chamber 2-9, the second evaporation chamber 35 and the ninth evaporation chamber 2-9, the top parts of the eight 2-8 steaming chamber and the seven 2-7 steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the seven 2-7 steaming chamber and the six 2-6 steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the six 2-6 steaming chamber and the five 2-5 steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the five 2-5 steaming chamber and the four 2-4 steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the four 2-4 steaming chamber and the three 2-3 steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the steaming chamber III 2-3 and the steaming chamber II 2-2 are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, the top parts of the steaming chamber II 2-2 and the steaming chamber I2-1 are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve 37, a connecting pipeline between the pre-concentration circulating pump 10 and an inner pipe of the external heater 5 penetrates through a gas-liquid exchange chamber of the steaming chamber V2-5, the steaming chamber IV 2-4, the steaming chamber III 2-3, the steaming chamber II 2-2 and the steaming chamber I2-1, a steam inlet pipe 26 enters a self-cleaning exhaust evaporator 4 after passing through an interlayer of the external heater 5, the bottom part of the steaming chamber V2-8 is connected with the gas-barrier settler 3 through a pipeline, a circulating balance pump 30 is arranged on a connecting pipeline between the self-cleaning exhaust evaporator 4 and the gas-barrier settler 3, the self-cleaning type exhaust gas evaporator 4, the gas barrier settler 3 and the first impurity collecting box 27 are connected together through pipelines, the first steam refining chamber 2-1, the second steam refining chamber 2-2, the third steam refining chamber 2-3, the fourth steam refining chamber 2-4, the fifth steam refining chamber 2-5, the sixth steam refining chamber 2-6, the seventh steam refining chamber 2-7, the eighth steam refining chamber 2-8, the ninth steam refining chamber 2-9 and the tenth steam refining chamber 2-10 are connected together through pipelines with the first impurity collecting box 27, the first impurity collecting box 27 and the second impurity collecting box 28 are connected together through pipelines, the self-cleaning type exhaust gas evaporator 4 is respectively connected with the condensed water collecting and storing tank 8 and the pre-concentrated liquid circulating pump 10 through pipelines, the top of the self-cleaning type exhaust gas evaporator 4 is connected with the cooling water tank 25 through a pipeline provided with a Roots air extractor 29, the feeding pipe orifice of the concentrated liquid circulating pump 11 is arranged at the bottom of the tenth steam refining chamber 2-10, the discharging pipe 11 of the concentrated liquid circulating pump 11 is connected with the condensate collecting tank 2-7 through a pipeline of the six steam refining chamber 2-6 and a temporary concentrated liquid separator 21, the concentrated liquid separator 21 is connected with the concentrated liquid collecting tank 22, the concentrated liquid separator 21 and the concentrated liquid crystal liquid storage tank 22 are connected together through pipelines, the concentrated liquid separator 21, the vacuum pump 18 is communicated with a condensate recovery tank 32, a distillation chamber nine 2-9 and a distillation chamber ten 2-10 through interlayers of a vacuum generator 7 and an air corrosion eliminator 6 in sequence through pipelines, the cooling water tank 25 is communicated with the cooling water tank 25 through an inner pipe of the air corrosion eliminator 6 through a pipeline provided with a cooling pump 39, the cooling water tank 25 is communicated with the cooling water tank 25 through an interlayer of a heat exchanger 13 after passing through a gas-liquid exchange chamber of the distillation chamber eight 2-8, the distillation chamber nine 2-9 and the distillation chamber ten 2-10 through a pipeline provided with a distillation chamber cooling pump 31, and a cooling tower 16 is arranged outside the cooling water tank 25.
The preheating solid-liquid separator 1, the self-cleaning exhaust gas evaporator 4 and the solid-liquid separator 21 are externally provided with a gas-liquid mixing pump 12, and the vacuum generator 7 is provided with a refrigerating machine 17.
The using method of the multi-pass concentration and purification device is characterized by comprising the following steps:
(1) Firstly, raw materials to be processed are collected in a raw liquid storage tank 15, then the raw materials are conveyed into a filter 14 by a raw liquid conveying pump 9, the raw materials filtered by the filter 14 enter a preheating type solid-liquid separator 1, and impurities filtered by the filter 14 are conveyed into a second impurity collecting box 28;
(2) The heat source of the preheating type solid-liquid separator 1 is from a gas-liquid exchange chamber of eight 2-8 steaming chambers, nine 2-9 steaming chambers and ten 2-10 steaming chambers, a cooling water tank 25 passes through the gas-liquid exchange chambers of eight 2-8 steaming chambers, nine 2-9 steaming chambers and ten 2-10 steaming chambers through a pipeline provided with a cooling pump 31 of the steaming chambers, and then is communicated with the cooling water tank 25 per se through an interlayer of a heat exchanger 13, and the preheating type solid-liquid separator 1 is connected with a circulating pump 33 and an inner pipe of the heat exchanger 13 in series, so that the material in the preheating type solid-liquid separator 1 is heated through the heat exchanger 13;
(3) The circulating pump 33 sends the materials in the preheating type solid-liquid separator 1 to the pre-concentration circulating pump 10, and the pre-concentration circulating pump 10 primarily heats the materials in a gas-liquid exchange chamber of a steaming chamber five 2-5, a steaming chamber four 2-4, a steaming chamber three 2-3, a steaming chamber two 2-2 and a steaming chamber one 2-1, and then the materials enter an external heater 5 for further heating and then enter an evaporation bridge 35 in the steaming chamber one 2-1;
(4) The vacuum pump 18 is respectively communicated with the condensed water recovery tank 32, the nine 2-9 steaming chamber and the ten 2-10 steaming chamber through pipelines sequentially passing through interlayers of the vacuum generator 7 and the gas erosion eliminator 6, so that the condensed water recovery tank 32, the nine 2-9 steaming chamber and the ten 2-10 steaming chamber have the same vacuum degree; through the adjustment of the intelligent vacuum proportional valve 37, the vacuum degrees between nine 2-9 of the steaming chamber, eight 2-8 of the steaming chamber, seven 2-7 of the steaming chamber, six 2-6 of the steaming chamber, five 2-5 of the steaming chamber, four 2-4 of the steaming chamber, three 2-3 of the steaming chamber, two 2-2 of the steaming chamber and one 2-1 of the steaming chamber are sequentially reduced, so that under the action of negative pressure, materials sequentially enter nine 2-9 of the steaming chamber from 2-1 of the steaming chamber, two 2-2 of the steaming chamber, three 2-3 of the steaming chamber, four 2-4 of the steaming chamber, five 2-5 of the steaming chamber, six 2-6 of the steaming chamber, seven 2-7 of the steaming chamber and eight 2-8 of the steaming chamber through an evaporation bridge 35, materials in the first distillation chamber 2-1, the second distillation chamber 2-2, the third distillation chamber 2-3, the fourth distillation chamber 2-4, the fifth distillation chamber 2-5, the sixth distillation chamber 2-6, the seventh distillation chamber 2-7, the eighth distillation chamber 2-8, the ninth distillation chamber 2-9 and the tenth distillation chamber 2-10 are communicated with one another through a series pipe 36, and after coming out from an evaporation bridge 35, the solution in the materials in the first distillation chamber 2-1, the second distillation chamber 2-2, the third distillation chamber three 2-3, the fourth distillation chamber four 2-4, the fifth distillation chamber five 2-5, the sixth distillation chamber six-6, the seventh distillation chamber seven 2-7, the eighth distillation chamber eight 2-8, the ninth distillation chamber nine 2-9 and the tenth distillation chamber ten 2-10 is evaporated into a gas-liquid exchange chamber on the upper portion of a water collecting plate 34, in the gas-liquid exchange chamber, the solution is pre-cooled to form a liquid solution which stays on the water collecting plate 34, the liquid solution is sucked into a vacuum condensate water recovery tank 32 through a pipeline, and the liquid solution can be recovered and utilized;
(5) Then the materials pass through a pre-concentration circulating pump 10, a first distillation chamber 2-1, a second distillation chamber 2-2, a third distillation chamber 2-3, a fourth distillation chamber 2-4, a fifth distillation chamber 2-5, a sixth distillation chamber 2-6, a seventh distillation chamber 2-7, a eighth distillation chamber 2-8, a gas barrier settler 3, a circulating balance pump 30, a self-cleaning exhaust gas evaporator 4 and the pre-concentration circulating pump 10 to form a pre-concentration circulation; the materials form an enrichment cycle through an enrichment circulating pump 11, a nine steaming chamber 2-9 and a ten steaming chamber 2-10;
(6) After the material comes out through the thickening circulating pump 11, the crystal recovery box 23 is retrieved with the crystal to the entering crystal and the liquid separator 22 that need the crystallization separation, and the back is come out through the thickening circulating pump 11 to the material, and the entering thick liquid that does not need the crystallization is in the case 24 that keeps in temporary, and the concentrated material of product delivery pump 38 in the case 24 that keeps in temporary with the thick liquid is sent people solid-liquid separator 21, and the concentrated material of thick liquid output pump 20 in with solid-liquid separator 21 is sent people to thick liquid storage tank 19, accomplishes the concentrated purification of material.
The invention aims to provide a multi-pass concentration and purification device which is reasonable in structure, low in cost, energy consumption and emission, improves the clean production level of industrial production and pollution control industries, reduces pollutants, reduces energy consumption and saves operation cost.
The invention relates to a multi-pass concentration and purification device, which has the following advantages:
1. the energy consumption of heating is saved, the utilization rate of waste heat is high, the utilization rate of secondary steam reaches more than 95%, the gas-liquid exchange of evaporation overflow gas is considered, and the two functions of waste heat utilization and gas-liquid exchange are synchronously realized.
2. The vacuum negative pressure circulation evaporation has the advantages of low evaporation temperature, high evaporation efficiency, good adaptability of heating energy, low energy consumption, even heating by utilizing a waste heat source, energy conservation and emission reduction.
3. High concentration and purification yield and stable product quality.
4. The material causticization harm is small, the scale and dirt deposition is less, the service life is long, and the maintenance period is long.
5. The system has the advantages of few faults, good safety performance, stable operation, simple and convenient operation, and compatibility with remote control, and can realize the operation of man-machine separation control.
6. The electric energy consumption is saved, and the circulating evaporation is mainly completed by vacuum self-absorption flow guide.
7. The utilization rate of water resources is high, the PH value of condensed water generated by evaporation of the non-volatile liquid is between 7.2 and 7.5, the condensed water can be completely used for production and recycling, the temperature of the condensed water is between 75 and 85 ℃, and the heating energy consumption in recycling is saved.
8. The environment-friendly effect is good, the waste and sewage discharge is less, the generated waste recycling rate and collection rate are high, the cyclic utilization rate is high, and the resource consumption is reduced.
9. The intelligent degree is high, and the operation and safety guarantee of each system realize the full coverage of the intelligent technology.
10. Wide industrial application field and great applicability to liquid concentration and purification.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications derived therefrom are intended to be within the scope of the invention.

Claims (4)

1. The utility model provides a multipass concentration purification device, includes preheating-type solid-liquid separator (1), multipass steam refining room (2), enrichment circulating pump (11), filter (14) and stoste storage tank (15), its characterized in that: a stock solution delivery pump (9) is arranged between the filter (14) and the stock solution storage tank (15), the preheating type solid-liquid separator (1) and the filter (14) are connected together through a pipeline, the preheating type solid-liquid separator (1) and the filter (14) are connected together with a second sundries collecting box (28) through a pipeline, the second sundries collecting box (28) and the stock solution storage tank (15) are connected together through a pipeline, the preheating type solid-liquid separator (1), a circulating pump (33) and an inner pipe of the heat exchanger (13) are connected together in series, a pre-concentration circulating pump (10) is arranged on a pipeline between the preheating type solid-liquid separator (1) and an inner pipe of the external heater (5), the multi-pass steaming chamber (2) comprises a first steaming chamber (2-1), a second steaming chamber (2-2), a third steaming chamber (2-3), a fourth steaming chamber (2-4), a fifth steaming chamber (2-5), a sixth steaming chamber (2-6), a seventh steaming chamber (2-7), an eighth steaming chamber (2-8), a ninth steaming chamber (2-9) and a tenth steaming chamber (2-10), and the first steaming chamber (2-1), the second steaming chamber (2-2), the third steaming chamber (2-3), the fourth steaming chamber (2-4) and the tenth steaming chamber (2-10), the middle parts of a fifth steaming chamber (2-5), a sixth steaming chamber (2-6), a seventh steaming chamber (2-7), an eighth steaming chamber (2-8), a ninth steaming chamber (2-9) and a tenth steaming chamber (2-10) are provided with a water collecting plate (34), the water collecting plate (34) is connected with a condensate water recovery tank (32) through a connecting pipeline, the upper part of the water collecting plate (34) is a gas-liquid exchange chamber, and the lower part of the water collecting plate (34) is a vaporization separation chamber; the evaporation and distillation device is characterized in that the evaporation chamber I (2-1), the evaporation chamber II (2-2), the evaporation chamber III (2-3), the evaporation chamber IV (2-4), the evaporation chamber V (2-5), the evaporation chamber VI (2-6), the evaporation chamber VII (2-7), the evaporation chamber VIII (2-8) and the evaporation chamber IX (2-9) are internally provided with an evaporation bridge (35), the evaporation bridge (35) in the evaporation chamber IX (2-9) is connected with the bottom of the evaporation chamber VIII (2-8) through a pipeline, the evaporation bridge (35) in the evaporation chamber IX (2-8) is connected with the bottom of the evaporation chamber VII (2-7) through a pipeline, the evaporation bridge (35) in the evaporation chamber VII (2-7) is connected with the bottom of the evaporation chamber VI (2-6) through a pipeline, the evaporation bridge (35) in the evaporation chamber VI (2-6) is connected with the evaporation chamber IX (2-5) through a pipeline, the bottom of the evaporation chamber IX (2-4) is connected with the evaporation chamber IX (2-4) through a pipeline, the evaporation bridge (35) is connected with the bottom of the evaporation chamber IX (2-4) is connected with the evaporation chamber IX (4) through a pipeline, evaporate in the room three (2-3) of cooking and evaporate the bottom of the room two (2-2) and link together through the pipe connection, evaporate in the room two (2-2) evaporation bridge (35) and evaporate the bottom of the room one (2-1) and pass through the pipe connection together, evaporate in the room one (2-1) evaporation bridge (35) and the inner tube of external heater (5) and link together, evaporate the bottom of room nine (2-9) and the room ten (2-10) of cooking and connect together through tandem pipe (36), evaporate the top of room nine (2-9) and room eight (2-8) of cooking and link together through the vacuum connecting pipe that is equipped with intelligent vacuum proportional valve (37), evaporate the top of room eight (2-8) and room seven (2-7) of cooking and be equipped with intelligent vacuum proportional valve (37) through the vacuum connecting pipe that is equipped with intelligent vacuum proportional valve (37) together, evaporate room (2-7) and evaporate room six (6) of cooking and link together through the vacuum connecting pipe that the room 2-6) of room five vacuum connecting pipe (5) are equipped with the room of cooking and evaporate the vacuum connecting pipe (5) and link together the room top of room 2-6) of cooking and five vacuum connecting pipe (5) of cooking and evaporate the room are equipped with the room vacuum connecting pipe (2-6) of cooking and connect together through the room vacuum connecting pipe (2-6) of the room The air connecting pipes are connected together, the tops of the four (2-4) and the three (2-3) steaming chambers are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve (37), the tops of the three (2-3) and the two (2-2) steaming chambers are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve (37), the tops of the two (2-2) steaming chambers and the one (2-1) steaming chamber are connected together through a vacuum connecting pipe provided with an intelligent vacuum proportional valve (37), a connecting pipeline between the pre-concentration circulating pump (10) and an inner pipe of the external heater (5) penetrates through a gas-liquid exchange chamber of the five (2-5) steaming chambers, the four (2-4) steaming chambers, the three (2-3) steaming chambers, the two (2-2) steaming chambers and the one (2-1) steaming chambers, a steam inlet pipe (26) enters the self-cleaning type exhaust gas evaporator (4) after passing through an interlayer of the external heater (5), the eight (2-8) steaming chambers are connected together with the air-blocking evaporator (3), and the air-blocking type self-cleaning evaporator (3) through an air blocking pipe (27), and the air-collecting tank (3), the bottom of the first steaming chamber (2-1), the second steaming chamber (2-2), the third steaming chamber (2-3), the fourth steaming chamber (2-4), the fifth steaming chamber (2-5), the sixth steaming chamber (2-6), the seventh steaming chamber (2-7), the eighth steaming chamber (2-8), the ninth steaming chamber (2-9) and the tenth steaming chamber (2-10) are connected with a first sundries collecting box (27) through pipelines, the first sundries collecting box (27) and the second sundries collecting box (28) are connected together through pipelines, the self-cleaning type exhaust gas evaporator (4) is respectively connected with a condensed water collecting box (8) and a pre-concentration circulating pump (10) through pipelines, the top of the self-cleaning type exhaust gas evaporator (4) is connected with a cooling water tank (25) through a pipeline provided with a Roots air extractor (29), a feeding pipe orifice of the concentration circulating pump (11) is arranged at the bottom of the tenth steaming chamber (2-10), a discharging pipe orifice of the concentration circulating pump (11) is communicated with a liquid exchange chamber (2-9) of the ninth steaming chamber (2-10) and a concentrate liquid exchange chamber (2-9) of the concentrate circulating pump (10), the concentrated solution temporary storage tank (24) is communicated with a solid-liquid separator (21) through a pipeline provided with a product conveying pump (38), the solid-liquid separator (21) is communicated with a concentrated solution storage tank (19) through a pipeline provided with a concentrated solution output pump (20), a crystal and liquid separator (22) is connected with a crystal recovery tank (23) through a pipeline, the crystal and liquid separator (22) and the solid-liquid separator (21) are connected together through a pipeline, a vacuum pump (18) is communicated with a condensate recovery tank (32), a distillation chamber nine (2-9) and a distillation chamber ten (2-10) through an interlayer of a vacuum generator (7) and an air corrosion eliminator (6) sequentially through pipelines, a cooling water tank (25) is communicated with the cooling water tank (25) through an inner pipe of the air corrosion eliminator (6) through a pipeline provided with a cooling pump (39), the cooling water tank (25) is communicated with the cooling water tank (25) through a pipeline provided with a distillation chamber cooling pump (31) through a distillation chamber eight (2-8), a distillation chamber nine (2-9) and a distillation chamber ten water tank (10), and a cooling water tank (25) is communicated with a cooling water tank (16) through a cooling water tank (16) outside the cooling tower.
2. The multi-pass concentration and purification device of claim 1, wherein: and a gas-liquid mixing pump (12) is arranged outside the preheating type solid-liquid separator (1), the self-cleaning type exhaust gas evaporator (4) and the solid-liquid separator (21).
3. The multi-pass concentration and purification device of claim 1, wherein: the vacuum generator (7) is provided with a refrigerator (17).
4. The method of claim 1, comprising the steps of:
(1) Firstly, raw materials to be processed are collected in a raw liquid storage tank (15), then the raw materials are conveyed into a filter (14) by a raw liquid conveying pump (9), the raw materials filtered by the filter (14) enter a preheating type solid-liquid separator (1), and impurities filtered by the filter (14) are conveyed into a second impurity collecting box (28);
(2) The heat source of the preheating type solid-liquid separator (1) is from a gas-liquid exchange chamber of a steaming chamber eight (2-8), a steaming chamber nine (2-9) and a steaming chamber ten (2-10), a cooling water tank (25) passes through the gas-liquid exchange chambers of the steaming chamber eight (2-8), the steaming chamber nine (2-9) and the steaming chamber ten (2-10) through a pipeline provided with a steaming chamber cooling pump (31) and then is communicated with the cooling water tank (25) through an interlayer of a heat exchanger (13), the preheating type solid-liquid separator (1) is connected with a circulating pump (33) and an inner pipe of the heat exchanger (13) in series, and thus the material in the preheating type solid-liquid separator (1) is heated through the heat exchanger (13);
(3) The circulating pump (33) sends the materials in the preheating type solid-liquid separator (1) to the pre-concentration circulating pump (10), and the pre-concentration circulating pump (10) primarily heats the materials through a gas-liquid exchange chamber of a fifth steaming chamber (2-5), a fourth steaming chamber (2-4), a third steaming chamber (2-3), a second steaming chamber (2-2) and a first steaming chamber (2-1), further heats the materials in the external heater (5), and then enters an evaporation bridge (35) in the first steaming chamber (2-1);
(4) The vacuum pump (18) is respectively communicated with the condensate water recovery tank (32), the steaming chamber nine (2-9) and the steaming chamber ten (2-10) through pipelines sequentially passing through interlayers of the vacuum generator (7) and the air erosion eliminator (6), so that the condensate water recovery tank (32), the steaming chamber nine (2-9) and the steaming chamber ten (2-10) have the same vacuum degree; through the adjustment of an intelligent vacuum proportional valve (37), the vacuum degrees between a nine (2-9) steaming chamber, an eight (2-8) steaming chamber, a seven (2-7) steaming chamber, a six (2-6) steaming chamber, a five (2-5) steaming chamber, a four (2-4) steaming chamber, a three (2-3) steaming chamber, a two (2-2) steaming chamber and a one (2-1) steaming chamber are sequentially reduced, so that under the action of negative pressure, materials sequentially enter a nine (2-9) steaming chamber from a first steaming chamber (2-1), a second steaming chamber (2-2), a third steaming chamber (2-3), a fourth steaming chamber (2-4), a fifth steaming chamber (2-5), a sixth steaming chamber (2-6), a seventh steaming chamber (2-7) and an eighth steaming chamber (2-8) through an evaporation bridge (35), the materials in the nine (2-9) steaming chamber and the ten (2-10) steaming chamber are communicated with each other through a series pipe (36), and the first steaming chamber (2-1), the second steaming chamber (2-2), the third steaming chamber (2-3), the fourth steaming chamber (2-4), the fifth steaming chamber (2-5), the sixth steaming chamber (2-6), the seventh steaming chamber (2-7), after coming out of an evaporation bridge (35), the solution in the materials in the eight (2-8) steaming chamber, the nine (2-9) steaming chamber and the ten (2-10) steaming chamber is evaporated into a gas-liquid exchange chamber at the upper part of a water collecting plate (34), in the gas-liquid exchange chamber, the solution steam is precooled to form liquid solution which stays on the water collecting plate (34), the liquid solution on the water collecting plate (34) can be sucked into a vacuum condensate water recovery tank (32) through a pipeline, and the liquid solution can be recovered for use;
(5) Then the materials form preconcentration circulation through a preconcentration circulation pump (10), a first steaming chamber (2-1), a second steaming chamber (2-2), a third steaming chamber (2-3), a fourth steaming chamber (2-4), a fifth steaming chamber (2-5), a sixth steaming chamber (2-6), a seventh steaming chamber (2-7), an eighth steaming chamber (2-8), a gas barrier settler (3), a circulation balance pump (30), a self-cleaning type exhaust gas evaporator (4) and the preconcentration circulation pump (10); the materials form an enrichment cycle through an enrichment cycle pump (11), a nine (2-9) steaming chamber and a ten (2-10) steaming chamber;
(6) The material through add concentration circulating pump (11) back of coming out, need the entering crystal and the liquid separator (22) of crystallization separation, retrieve crystal collection box (23) with the crystal, the material is through adding concentration circulating pump (11) back of coming out, in the entering concentrate temporary storage box (24) that does not need the crystallization, product delivery pump (38) send the concentrated material in concentrate temporary storage box (24) people solid-liquid separation ware (21), concentrate output pump (20) send the concentrated material in solid-liquid separation ware (21) people concentrate storage tank (19), accomplish the concentrated purification of material.
CN201711413470.0A 2017-12-24 2017-12-24 Multi-pass concentration and purification device and using method thereof Active CN107854857B (en)

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US2544885A (en) * 1946-02-27 1951-03-13 Gen Am Transport Vertical tube evaporator
JPH10249101A (en) * 1997-03-13 1998-09-22 Kooyo Techno Kk Liqiud concentrator
WO2005056150A2 (en) * 2003-12-03 2005-06-23 Arizona Board Of Regents Method and apparatus for simultaneous heat and mass transfer utilizing a carrier-gas at various absolute pressures
CN203425541U (en) * 2013-08-13 2014-02-12 南宁市科潮酒精技术开发有限责任公司 Multiple-effect evaporation and concentration integrated equipment for molasses alcohol fermented mature undecanted wine
CN203540090U (en) * 2013-10-15 2014-04-16 济南华明生化有限公司 Itaconic acid energy-saving-type four-effect concentrating and crystallizing device
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CN207734624U (en) * 2017-12-24 2018-08-17 无锡诚尔鑫环保装备科技有限公司 A kind of multi-way concentration purifying plant

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