CN113856219A - Low-temperature normal-pressure evaporation device and evaporation process thereof - Google Patents
Low-temperature normal-pressure evaporation device and evaporation process thereof Download PDFInfo
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- CN113856219A CN113856219A CN202111219392.7A CN202111219392A CN113856219A CN 113856219 A CN113856219 A CN 113856219A CN 202111219392 A CN202111219392 A CN 202111219392A CN 113856219 A CN113856219 A CN 113856219A
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- 238000001704 evaporation Methods 0.000 title claims abstract description 137
- 230000008020 evaporation Effects 0.000 title claims abstract description 137
- 238000000034 method Methods 0.000 title claims abstract description 55
- 238000010438 heat treatment Methods 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 31
- 239000007788 liquid Substances 0.000 claims abstract description 28
- 238000007599 discharging Methods 0.000 claims abstract description 20
- 239000002904 solvent Substances 0.000 claims abstract description 8
- 238000000926 separation method Methods 0.000 claims abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 239000000945 filler Substances 0.000 claims description 30
- 239000012071 phase Substances 0.000 claims description 28
- 229920006395 saturated elastomer Polymers 0.000 claims description 25
- 239000007921 spray Substances 0.000 claims description 23
- 239000012943 hotmelt Substances 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 8
- 239000007791 liquid phase Substances 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 6
- 239000013589 supplement Substances 0.000 claims description 6
- 230000000630 rising effect Effects 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000004134 energy conservation Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 23
- 238000005516 engineering process Methods 0.000 description 7
- 150000003839 salts Chemical class 0.000 description 6
- 239000002351 wastewater Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000007769 metal material Substances 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 235000011152 sodium sulphate Nutrition 0.000 description 3
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 230000003631 expected effect Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052755 nonmetal Inorganic materials 0.000 description 2
- 239000011780 sodium chloride Substances 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 241000282414 Homo sapiens Species 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000001174 ascending effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0082—Regulation; Control
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/0094—Evaporating with forced circulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/30—Accessories for evaporators ; Constructional details thereof
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a low-temperature normal-pressure evaporation device and an evaporation process thereof, and the evaporation device comprises an evaporation tower, wherein a low-temperature evaporation assembly is arranged at the upper part of the evaporation tower, one side of the low-temperature evaporation assembly is connected with a solution heating device, one side of the evaporation tower is connected with a gas-phase cooling device, the top of the evaporation tower is connected with an air circulating device, the solution heating device is communicated with the gas-phase cooling device, the gas-phase cooling device is communicated with the air circulating device, and the bottom of the evaporation tower is connected with a discharging device. The invention fully utilizes the surplus low-grade heat source in the factory, realizes the separation of the solute and the solvent at low temperature and normal pressure, realizes the zero discharge of liquid, and recycles the solute components in the solvent. Not only protects the environment, but also utilizes the low-grade heat source resource which is difficult to utilize, thereby achieving the purpose of energy conservation.
Description
Technical Field
The invention relates to the technical field of low-temperature evaporation, in particular to a low-temperature normal-pressure evaporation device and an evaporation process thereof.
Background
In recent years, industrial science and technology are continuously developed, abundant material basic support is provided for convenient living conditions of people, and more energy supplies are consumed for the convenient living conditions; the annual increasing petrochemical energy consumption has caused real, global climate problems, even the frequent occurrence of catastrophic climates in local areas; the climate problem is the most urgent problem that human beings face together all the time, and is one of the biggest cooperation subjects of countries in history.
Before renewable energy sources are widely used for replacing petrochemical energy sources, clean energy sources and energy-saving technology are important ways for improving climate change, and the clean energy sources widely replace traditional petrochemical energy sources to carry out the most successful case of large-scale environmental management, namely one of the methods for haze management in North China, so that a good effect is achieved; in addition to the adjustment of a primary energy use structure, the energy-saving and emission-reducing technology of a user is adopted, in the industry, the consumption of the chemical industry and the metal product manufacturing industry on the production and supply of electric power and steam hot water is far larger than that of other departments, the production of the steam and the hot water needs a large amount of energy, the steam consumption in the chemical industry is the largest through rectification, evaporation and drying, and the energy-saving and emission-reducing technology is still an important energy-saving control means before subversive processes are not used for replacing the high-energy-consumption processes.
In the evaporation industry, a plurality of evaporation technologies such as MEE, TVR and MVR exist, and the energy-saving effect is obvious for different users, especially in the salt-containing wastewater zero-discharge industry, so that the method is widely applied. Similarly, these evaporation techniques also have obvious disadvantages, the evaporation temperature is above the boiling point, the operation temperature is high, the pressure is low, a higher vacuum degree is required, the salt corrosion resistance, the strength and the like of the equipment are higher requirements, and only expensive metal materials can be selected to manufacture the equipment, for example, the MVR technique has high requirements on a vapor compressor, which finally causes the disadvantages of high investment, high operation cost, more complex equipment maintenance, easy scaling of metal and the like of the traditional evaporation technique. Moreover, the MVR evaporation technology with low steam quality requirement is used, saturated steam with 0.2Mpa is required for supplementing steam, and a large amount of low-quality heat sources in a factory, such as secondary steam, steam exhaust, hot water and other low heat energy cannot be effectively utilized, so that the overall thermal efficiency of the factory is low, and the energy consumption of final products is high.
In recent years, the environmental protection pressure of the chemical industry is increased year by year, the national carbon emission reduction plan is further executed, clean emission is realized while the energy supply is reduced, and higher requirements are put forward on the gradient utilization of energy in the industry, so that a low-temperature normal-pressure evaporation technology is urgently needed to fully utilize the low-quality heat source of a factory.
Disclosure of Invention
The invention aims to solve the technical problems and provides a low-temperature normal-pressure evaporation device and an evaporation process thereof.
In order to achieve the technical purpose and achieve the technical requirements, the invention adopts the technical scheme that: a low-temperature normal-pressure evaporation device is characterized in that: the device comprises an evaporation tower, wherein a low-temperature evaporation assembly is arranged at the upper part of the evaporation tower, one side of the low-temperature evaporation assembly is connected with a solution heating device, one side of the evaporation tower is connected with a gas-phase cooling device, the top of the evaporation tower is connected with an air circulating device, the solution heating device is communicated with the gas-phase cooling device, the gas-phase cooling device is communicated with the air circulating device, and the bottom of the evaporation tower is connected with a discharging device;
the solution heating device comprises a fifth heat exchanger, the fifth heat exchanger is communicated with the feeding pipeline, and a steam inlet and a condensate outlet are formed in the fifth heat exchanger;
the low-temperature evaporation assembly comprises a filler and a spray gun, the filler is arranged in the evaporation tower, and one end of the spray gun penetrates through the side wall of the evaporation tower and is connected with the solution heating device through a pipeline;
the gas phase cooling device comprises a first heat exchanger, one side of the first heat exchanger is communicated with a fifth heat exchanger, the other side of the first heat exchanger is communicated with the evaporation tower through a circulating pump, the first heat exchanger is connected with a second heat exchanger through a circulating pipeline, and a hot working medium outlet of the first heat exchanger is communicated with a hot working medium inlet of the second heat exchanger through a working medium buffer tank and a working medium pump; the heat source inlet of the second heat exchanger is communicated with the evaporation tower through a pipeline, a water retainer is arranged on the pipeline, the heat source outlet of the second heat exchanger is connected with the heat source inlet of a third heat exchanger through a pipeline, a cold source inlet is arranged on one side of the third heat exchanger, the cold source outlet of the third heat exchanger is connected with a fourth heat exchanger, and drain ports of the second heat exchanger and the third heat exchanger are connected with a clean water storage tank through pipelines;
the air circulating device comprises a fourth heat exchanger, a cold source inlet of the fourth heat exchanger is connected with a heat source outlet of the third heat exchanger, a cold source outlet of the fourth heat exchanger is connected with the evaporation tower (2) through a circulating fan, and a heat source outlet is arranged on one side of the fourth heat exchanger;
discharging device includes the discharge pump, discharge pump one side is linked together with evaporation tower bottom, and the opposite side is linked together with ejection of compact pipeline.
Preferably: the filler sets up to the multilayer and packs, the spray gun sets up to the multiunit spray gun, the multilayer packs and multiunit spray gun interval sets up.
The evaporation process of the low-temperature normal-pressure evaporation device is characterized in that: the method comprises the following steps:
a. a solution heating procedure: the raw solution enters a solution heating device through a feeding pipeline, meanwhile, steam enters the solution heating device through a steam inlet to exchange heat with the raw solution, and the solution heating device transfers more than 90% of energy in the steam to the raw solution to heat the raw solution;
b. solution evaporation process: the heated hot solution enters the low-temperature evaporation assembly, meanwhile, the cold air A enters the low-temperature evaporation assembly, the hot melt liquid and the cold air A carry out rapid heat exchange in the low-temperature evaporation assembly, water molecules in the hot melt liquid are rapidly diffused in the cold air A, the cold air A reaches a saturated water-containing state and is converted into saturated humid hot air, after the hot solution is evaporated, the concentrated solution flows to the bottom of the evaporation tower, when the subsequent cold air enters, the solvent in the solution is diffused and evaporated to the cold air, the temperature of the hot melt liquid is reduced to be the cold solution, and the energy and the material are transferred from the liquid phase to the gas phase;
c. a gas-phase cooling process: the cold solution enters a gas phase cooling device, the cooled cold solution and saturated damp and hot air are subjected to heat exchange in the gas phase cooling device to finish energy transfer from a gas phase to a liquid phase, the heated and heated cold solution enters a solution heating device to supplement heat required by a solution heating process, then the cold solution enters an evaporation tower for circulation, the cold air B with the reduced temperature enters an air circulation device, and condensed water obtained by cooling and condensation enters a collection system;
d. an air circulation process: the cold air B is converted into cold air A by recovering the heat of the system to the maximum extent through an air circulating device, and then enters an evaporation tower for circulation;
e. a discharging procedure: when the concentration ratio of the concentrated solution in the evaporation tower reaches a set range, the discharge pump is started to discharge the concentrated solution out of the system.
Preferably: in the step a, the heating temperature of the original solution is set to be 40-90 ℃.
Preferably: in the step b, the heated hot solution is uniformly dispersed on the filler by a spray gun, and the spraying density is set to be 5-15m3/m2H, setting the temperature of cold air A entering the evaporation tower to be 20-60 ℃, setting the circulation speed of the cold air A to be 0.5-5m/s, and directly contacting the cold air A and the hot solution on the surfaces of the micro-droplets to finish the mass and heat transfer process.
Preferably: in the step c, cold solution enters a first heat exchanger through a circulating pump, circulates between the first heat exchanger and a second heat exchanger, saturated damp and hot air enters the first heat exchanger through the second heat exchanger and circulates between the first heat exchanger and the second heat exchanger, the circulated cold solution and the saturated damp and hot air exchange heat in the first heat exchanger, and the saturated damp and hot air after heat exchange is converted into damp and hot air; the heat is transferred to a second heat exchanger by a hot working medium through a working medium buffer pump and a working medium pump, the cold solution and the hot working medium carry out secondary heat transfer in the second heat exchanger, the cold solution heated by the first heat exchanger and the second heat exchanger enters a fifth heat exchanger to supplement the heat required by the solution heating process, and then enters an evaporation tower for circulation; the damp and hot air enters the third heat exchanger from the heat source outlet of the second heat exchanger, meanwhile, the cold medium enters from the cold source inlet, the rising damp and hot air exchanges heat with the cold medium, the cooled damp and hot air is condensed out of condensed water and is converted into cold air B, and the cold medium absorbs heat and enters the fourth heat exchanger.
Preferably: and d, enabling the cold air B to enter a fourth heat exchanger to exchange heat with a cold medium absorbing heat by the third heat exchanger, converting the heat absorbed by the cold air B into cold air A, pushing the cold air A into an evaporation tower to circulate as a separation working medium by a circulating fan, and discharging the cold medium from a heat source outlet of the fourth heat exchanger.
Compared with the traditional structure, the invention has the beneficial effects that:
1. the invention fully utilizes the surplus low-grade heat source in the factory, realizes the separation of the solute and the solvent at low temperature and normal pressure, realizes the zero discharge of liquid, and recycles the solute components in the solvent. Not only protects the environment, but also utilizes the low-grade heat source resource which is difficult to utilize, thereby achieving the purpose of energy conservation.
2. The invention has wide application range and strong applicability, can be used singly or in combination in the occasions of seawater desalination, salt-containing wastewater evaporative concentration, salt-containing COD wastewater evaporative concentration, thermosensitive material evaporative concentration, salt-containing wastewater evaporative crystallization, salt-containing COD wastewater evaporative crystallization and the like, can fully utilize low-quality waste heat of factories, and can be used under the special condition without low-quality heat sources.
3. The invention has low operation cost and no scaling risk, the evaporation at low temperature and normal pressure is mostly finished at about 60 ℃, the requirement on the material of the device is not high, the nonmetal material can be used for replacing expensive metal materials, the corrosion resistance of the nonmetal material is far higher than that of the metal material, the defects of easy corrosion and easy scaling of the metal material are overcome, and the operation cost is reduced.
4. The invention has stable and reliable operation, convenient maintenance and high evaporation efficiency, reduces the intensity requirement on evaporation equipment by directly contacting gas and liquid under the environment of low temperature and normal pressure, reduces heat exchange equipment, fully utilizes low-grade waste heat in the industry, and can separate solute from solvent in solution with good efficiency in a short time.
Drawings
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a process flow diagram of a 100kg/h low-temperature atmospheric vaporization system according to an embodiment of the present invention;
in the figure: 1. the device comprises a discharge pump, 2 an evaporation tower, 3 a fifth heat exchanger, 4 filler, 5 a spray gun, 6 a circulating fan, 7 a fourth heat exchanger, 8 a third heat exchanger, 9 a second heat exchanger, 10 a water eliminator, 11 a working medium buffer tank, 12 a working medium pump, 13 a circulating pump and 14 a first heat exchanger.
Detailed Description
The present invention is further described below.
Referring to the attached drawings, the low-temperature normal-pressure evaporation device is characterized in that: the device comprises an evaporation tower 2, wherein a low-temperature evaporation assembly is arranged at the upper part of the evaporation tower 2, one side of the low-temperature evaporation assembly is connected with a solution heating device, one side of the evaporation tower 2 is connected with a gas phase cooling device, the top of the evaporation tower 2 is connected with an air circulating device, the solution heating device is communicated with the gas phase cooling device, the gas phase cooling device is communicated with the air circulating device, and the bottom of the evaporation tower 2 is connected with a discharging device;
the solution heating device comprises a fifth heat exchanger 3, the fifth heat exchanger 3 is communicated with a feeding pipeline, and a steam inlet and a condensate outlet are formed in the fifth heat exchanger 3;
the low-temperature evaporation assembly comprises a filler 4 and a spray gun 5, the filler 4 is arranged in the evaporation tower 2, and one end of the spray gun 5 penetrates through the side wall of the evaporation tower 2 and is connected with the solution heating device through a pipeline;
the gas phase cooling device comprises a first heat exchanger 14, one side of the first heat exchanger 14 is communicated with a fifth heat exchanger 3, the other side of the first heat exchanger is communicated with the evaporation tower 2 through a circulating pump 13, the first heat exchanger 14 is connected with the second heat exchanger 9 through a circulating pipeline, and a hot working medium outlet of the first heat exchanger 14 is communicated with a hot working medium inlet of the second heat exchanger 9 through a working medium buffer tank 11 and a working medium pump 12; a heat source inlet of the second heat exchanger 9 is communicated with the evaporation tower 2 through a pipeline, a water retainer 10 is arranged on the pipeline, a heat source outlet of the second heat exchanger 9 is connected with a heat source inlet of a third heat exchanger 8 through a pipeline, a cold source inlet is arranged on one side of the third heat exchanger 8, a cold source outlet of the third heat exchanger 8 is connected with a fourth heat exchanger 7, and drain ports of the second heat exchanger 9 and the third heat exchanger 8 are connected with a clean water storage tank through pipelines;
the air circulating device comprises a fourth heat exchanger 7, a cold source inlet of the fourth heat exchanger 7 is connected with a heat source outlet of a third heat exchanger 8, a cold source outlet of the fourth heat exchanger 7 is connected with the evaporation tower 2 through a circulating fan 6, and a heat source outlet is arranged on one side of the fourth heat exchanger 7;
the discharging device comprises a discharging pump 1, one side of the discharging pump 1 is communicated with the bottom of the evaporation tower 2, and the other side of the discharging pump is communicated with a discharging pipeline.
In the preferred embodiment, the filler 4 is provided as a plurality of layers of fillers, the spray guns 5 are provided as a plurality of groups of spray guns, and the plurality of layers of fillers and the plurality of groups of spray guns are arranged at intervals.
The evaporation process of the low-temperature normal-pressure evaporation device is characterized in that: the method comprises the following steps:
a. a solution heating procedure: the raw solution enters a solution heating device through a feeding pipeline, meanwhile, steam enters the solution heating device through a steam inlet to exchange heat with the raw solution, and the solution heating device transfers more than 90% of energy in the steam to the raw solution to heat the raw solution;
b. solution evaporation process: the heated hot solution enters the low-temperature evaporation assembly, meanwhile, the cold air A enters the low-temperature evaporation assembly, the hot melt liquid and the cold air A carry out rapid heat exchange in the low-temperature evaporation assembly, water molecules in the hot melt liquid are rapidly diffused in the cold air A, the cold air A reaches a saturated water-containing state and is converted into saturated humid hot air, after the hot melt liquid is evaporated, the concentrated liquid flows to the bottom of the evaporation tower, when the subsequent cold air enters, the solvent in the solution is diffused and evaporated to the cold air, the temperature of the hot melt liquid is reduced to be the cold solution, and the energy and the substances are transferred from the liquid phase to the gas phase;
c. a gas-phase cooling process: the cold solution enters a gas phase cooling device, the cooled cold solution and saturated damp and hot air are subjected to heat exchange in the gas phase cooling device to finish energy transfer from a gas phase to a liquid phase, the heated and heated cold solution enters a solution heating device to supplement heat required by a solution heating process, then the cold solution enters an evaporation tower for circulation, the cold air B with the reduced temperature enters an air circulation device, and condensed water obtained by cooling and condensation enters a collection system;
d. an air circulation process: the cold air B is converted into cold air A by recovering the heat of the system to the maximum extent through an air circulating device, and then enters an evaporation tower for circulation;
e. a discharging procedure: when the concentration ratio of the concentrated solution in the evaporation tower reaches a set range, the discharge pump is started to discharge the concentrated solution out of the system.
In the preferred embodiment, in the step a, the heating temperature of the raw solution is set to 40-90 ℃.
In the preferred embodiment, in the step b, the heated hot solution is uniformly dispersed on the filler 4 by the spray gun 5, and the spray density is set to be 5-15m3/m2H, setting the temperature of cold air A entering the evaporation tower 2 to be 20-60 ℃, setting the circulation speed of the cold air A to be 0.5-5m/s, and directly contacting the cold air A and the hot solution on the surfaces of the micro-droplets to finish the mass and heat transfer process.
In the preferred embodiment, in the step c, the cold solution enters the first heat exchanger 14 through the circulating pump 13, circulates between the first heat exchanger 14 and the second heat exchanger 9, the saturated humid hot air enters the first heat exchanger 14 through the second heat exchanger 9, circulates between the first heat exchanger 9 and the second heat exchanger 14, the circulated cold solution and the saturated humid hot air exchange heat in the first heat exchanger 14, and the saturated humid hot air after heat exchange is converted into humid hot air; heat is transferred to the second heat exchanger 9 from the hot working medium through the working medium buffer pump 11 and the working medium pump 12, the cold solution and the hot working medium carry out secondary heat transfer in the second heat exchanger 9, the cold solution heated and heated by the first heat exchanger 14 and the second heat exchanger 9 enters the fifth heat exchanger 3, heat required by the solution heating process is supplemented, and then the cold solution enters the evaporation tower 2 for circulation; the damp and hot air enters the third heat exchanger 8 from the heat source outlet of the second heat exchanger 9, meanwhile, the cold medium enters from the cold source inlet, the rising damp and hot air exchanges heat with the cold medium, the cooled damp and hot air is condensed out of condensed water and is converted into cold air B, and the cold medium absorbs heat and enters the fourth heat exchanger 7.
In the preferred embodiment, in the step d, the cold air B enters the fourth heat exchanger 7 to exchange heat with the cold medium of the third heat exchanger absorbing heat, the cold air B absorbs heat and is converted into the cold air a, the cold air a is pushed by the circulating fan 6 to enter the evaporation tower 2 to circulate as the separation working medium, and the cold medium is discharged from the heat source outlet of the fourth heat exchanger 7.
Example 1:
a100 kg/h pilot plant evaporates and concentrates the sodium chloride solution, the sodium chloride content is 18% +/-0.3%, and the concentration is carried out to saturation. In the specific implementation process, the optimal circulating wind speed is 1.5-2.5m/s, the spraying density is 9-11.5 m/h, the chlorine root content of the condensate after evaporation is less than 100ppm, the water quality is clear, the low-grade steam supplement amount is less than 0.25t/t, and the evaporation reaches the expected effect of design.
Example 2:
the 100kg/h pilot plant is used for treating the sodium sulfate wastewater, the sodium sulfate content is 3.6-5%, the COD content is 1200-1500ppm, and the hardness is less than or equal to 150. In the specific implementation process, the preferable circulating wind speed is 1.5-2.5m/s, the spraying density is 10-12 m/h, the sulfate content of the evaporated condensate is less than 100ppm, the COD is less than 300ppm, the water quality is clear, and the COD of the sodium sulfate product separated by a centrifuge is as follows: 18000ppm, further treatment, low grade steam supply with evaporation amount less than 0.19t/t, and evaporation reaching the expected effect.
During the specific implementation, the invention simulates the evaporation and rainfall process in an independent system under the low-temperature normal-pressure environment, simultaneously generates the transfer of energy and substances, directly contacts gas and liquid through the continuous circulating gas in the device and the stage temperature change thereof, limits the gas flow rate to 0.5-5m/s, limits the liquid flow rate to 5-15 m/square meter h relative to the spraying density of the filler, controls the evaporation temperature to 40-90 ℃, diffuses water in the liquid state into the gas through gas-liquid countercurrent or cocurrent direct contact when the solution is evaporated in the evaporation system, condenses the water in the gas state into cooling water through a high heat conduction heat exchanger when the cooling system is cooled, and recycles the heat.
A solution heating procedure: conveying the original solution to a hot gas phase-solution heat exchanger (a fifth heat exchanger 3) through a conveying pump, transferring more than 90% of energy in steam to the original solution through the hot gas phase-solution heat exchanger (the fifth heat exchanger 3), and supplementing the rest of heat by low-grade heat source-solution heat exchangers (a first heat exchanger 14 and a second heat exchanger 9);
solution evaporation process: the heated solution is spread on the filler by a spray gun after the temperature reaches 40-90 ℃, the solution naturally and uniformly infiltrates the surface of the filler under the action of gravity, the spray density is 5-15 m/square meter.h, cold air A at 20-60 ℃ enters from the top (or the bottom) of the tower, the speed is 0.5-5m/s, the descending (or ascending) cold air A and the hot solution directly contact with each other in a concurrent (or countercurrent) way on the surface of the filler to finish the mass and heat transfer process, the process is carried out simultaneously, the enthalpy of the hot solution A is transferred to the cold air A, the temperature of the hot solution is reduced to be changed into the cold solution, the temperature of the cold air A is increased, the absolute saturated water content of the cold air A is increased along with the temperature increase, the water in the hot solution simultaneously escapes into the air, the enthalpy of the cold air A passing through the filler is increased, and the absolute water content of the cold air A after the filler is discharged from the filler is increased, the solution is converted into saturated damp and hot air, the evaporation process of the solution is completed, the temperature of the saturated damp and hot air is increased by 10-30 ℃ compared with that of cold air A, and the hot solution A takes away a large amount of heat due to the diffusion of water from a liquid state to a gas state so as to be converted into cold solution;
a gas-phase cooling process: cold solution with the temperature reduced by 10-30 ℃ enters a first heat exchanger 14 through a circulating pump, circulates between the first heat exchanger 14 and a second heat exchanger 9, the circulated cold solution and saturated damp-hot air exchange heat in the first heat exchanger to recover most of heat, the temperature of the saturated damp-hot air is reduced after heat exchange, part of condensed water is condensed and converted into damp-hot air, in addition, after heat exchange is carried out in the first heat exchanger 14, the heat is transferred to the second heat exchanger 9 through a hot working medium, in the second heat exchanger 9, the cold solution and the hot working medium exchange heat again, the cold solution after heat exchange and temperature rise through the first heat exchanger 14 and the second heat exchanger 9 enters a fifth heat exchanger 3 to supplement the heat required by the original solution heating process, and then enters an evaporation tower 2 for circulation; the wet and hot air with the reduced temperature enters a third heat exchanger 8, the temperature is about 40-60 ℃, the speed is 0.5-5m/s, the rising wet and hot air and cold media carry out heat transfer in the third heat exchanger 8, the process is carried out simultaneously, the wet and hot air transfers the enthalpy to the cold media, the temperature of the wet and hot air is reduced, the absolute saturated water content of the wet and hot air is reduced along with the temperature reduction, at the moment, the cooled wet and hot air is condensed out of condensed water, the condensed water enters a collection system, so that the enthalpy value of the wet and hot air passing through the third heat exchanger 8 is reduced and is converted into cold air B, the cold media transfers the heat to a fourth heat exchanger 7, the absolute water content of the cold air B after filling is reduced, and the cooling process of the wet and hot air is completed;
an air circulation process: the cold air B coming out of the third heat exchanger 8 enters the fourth heat exchanger 7, heat exchange is carried out on the cold air B and the heat transferred by the cold medium of the third heat exchanger 8 in the fourth heat exchanger 7, the cold air B absorbs partial heat and is converted into cold air A, and the cold air A is pushed by the circulating fan 6 to enter the evaporation tower 2 to be used as a separation working medium to circulate.
Spraying density: relatively to the filler, a spray density is in the range of from 5 to 15m square meter per square meter, preferably from 7 to 13m, more preferably from 9.5 to 11.5 m; when the lower limit is selected, the liquid on the surface of the filler is not well soaked, so that solute is deposited on the surface of the filler and even scaling is caused, and finally the efficiency is poor; when the upper limit is selected, splashing can be formed, more small droplets are formed and taken away by the airflow, the solute of the condensate exceeds the standard, the quality of the condensate is reduced, and finally the efficiency is poor; when a more optimal range is selected, the surface of the filler is well wetted, the washing of the precipitated solute of the filler is optimal, the optimal state of the surface of the filler is maintained with good efficiency, the splashing amount is small, more than 99% of splashed liquid drops can be blocked by the water eliminator, and finally the condensate has good solute content level and optimal efficiency.
Air circulation wind speed: in the closed system, the circulating wind speed is 0.5-5m/s, the range of 1-3m/s is preferred, and the range of 1.5-2.5m/s is more preferred; when the lower limit is selected, the gas-liquid direct contact heat exchange efficiency is low, and finally the overall efficiency is low; when the upper limit is selected, the gas-liquid direct contact heat exchange efficiency is increased, but the gas velocity is too high, so that the splashing liquid drop sedimentation is not facilitated, the efficiency of the water eliminator is reduced, the solute is increased in the condensate, the quality of the condensate is reduced, and the final efficiency is poor; when a more optimal range is selected, the gas-liquid direct contact thermal efficiency is good, the water eliminator can stop more than 99% of splashed liquid drops, and finally the condensate liquid solute content level is good and the efficiency is optimal.
Evaporation temperature: the feeding temperature of the hot solution is 40-90 ℃, and no preference is given; when the feeding temperature of the hot solution is too high, the requirement on equipment materials is higher, and the investment cost is not reduced.
Cooling air: the temperature of the mixture entering an evaporation tower is 20-60 ℃, and no preference is given; the difference is large in different regions, and cold air with lower temperature can be obtained more easily in the region with lower annual average temperature, so that gas-liquid countercurrent direct contact is facilitated to carry out heat exchange; in the area with higher average temperature in the year, cold air with lower temperature is obtained, and more energy needs to be paid out additionally.
Therefore, different applications, different low-quality heat sources, need to plan process details according to the thermal model to achieve the best thermal efficiency.
The above-mentioned embodiments of the present invention are only examples for clearly illustrating the present invention, but not intended to limit the scope of the present invention, and all equivalent technical solutions also belong to the scope of the present invention, and the scope of the present invention should be defined by the claims.
Claims (7)
1. A low-temperature normal-pressure evaporation device is characterized in that: the device comprises an evaporation tower (2), wherein a low-temperature evaporation assembly is arranged at the upper part of the evaporation tower (2), one side of the low-temperature evaporation assembly is connected with a solution heating device, one side of the evaporation tower (2) is connected with a gas-phase cooling device, the top of the evaporation tower (2) is connected with an air circulating device, the solution heating device is communicated with the gas-phase cooling device, the gas-phase cooling device is communicated with the air circulating device, and the bottom of the evaporation tower (2) is connected with a discharging device;
the solution heating device comprises a fifth heat exchanger (3), the fifth heat exchanger (3) is communicated with a feeding pipeline, and a steam inlet and a condensate outlet are formed in the fifth heat exchanger (3);
the low-temperature evaporation assembly comprises a filler (4) and a spray gun (5), the filler (4) is arranged in the evaporation tower (2), and one end of the spray gun (5) penetrates through the side wall of the evaporation tower (2) and is connected with a solution heating device through a pipeline;
the gas phase cooling device comprises a first heat exchanger (14), one side of the first heat exchanger (14) is communicated with a fifth heat exchanger (3), the other side of the first heat exchanger is communicated with the evaporation tower (2) through a circulating pump (13), the first heat exchanger (14) is connected with a second heat exchanger (9) through a circulating pipeline, and a hot working medium outlet of the first heat exchanger (14) is communicated with a hot working medium inlet of the second heat exchanger (9) through a working medium buffer tank (11) and a working medium pump (12); a heat source inlet of the second heat exchanger (9) is communicated with the evaporation tower (2) through a pipeline, a water retainer (10) is arranged on the pipeline, a heat source outlet of the second heat exchanger (9) is connected with a heat source inlet of a third heat exchanger (8) through a pipeline, a cold source inlet is arranged on one side of the third heat exchanger (8), a cold source outlet of the third heat exchanger (8) is connected with a fourth heat exchanger (7), and drain ports of the second heat exchanger (9) and the third heat exchanger (8) are connected with a clean water storage tank through pipelines;
the air circulating device comprises a fourth heat exchanger (7), a cold source inlet of the fourth heat exchanger (7) is connected with a heat source outlet of a third heat exchanger (8), a cold source outlet of the fourth heat exchanger (7) is connected with the evaporation tower (2) through a circulating fan (6), and a heat source outlet is arranged on one side of the fourth heat exchanger (7);
the discharging device comprises a discharging pump (1), one side of the discharging pump (1) is communicated with the bottom of the evaporation tower (2), and the other side of the discharging pump is communicated with a discharging pipeline.
2. The low-temperature normal-pressure evaporation device according to claim 1, wherein: the filler (4) is arranged into a plurality of layers of fillers, the spray guns (5) are arranged into a plurality of groups of spray guns, and the plurality of layers of fillers and the plurality of groups of spray guns are arranged at intervals.
3. The evaporation process using the low-temperature normal-pressure evaporation device according to claim 1, characterized in that: the method comprises the following steps:
a. a solution heating procedure: the raw solution enters a solution heating device through a feeding pipeline, meanwhile, steam enters the solution heating device through a steam inlet to exchange heat with the raw solution, and the solution heating device transfers more than 90% of energy in the steam to the raw solution to heat the raw solution;
b. solution evaporation process: the heated hot solution enters the low-temperature evaporation assembly, meanwhile, the cold air A enters the low-temperature evaporation assembly, the hot melt liquid and the cold air A carry out rapid heat exchange in the low-temperature evaporation assembly, water molecules in the hot melt liquid are rapidly diffused in the cold air A, the cold air A reaches a saturated water-containing state and is converted into saturated humid hot air, after the hot solution is evaporated, the concentrated solution flows to the bottom of the evaporation tower, when the subsequent cold air enters, the solvent in the solution is diffused and evaporated to the cold air, the temperature of the hot melt liquid is reduced to be the cold solution, and the energy and the material are transferred from the liquid phase to the gas phase;
c. a gas-phase cooling process: the cold solution enters a gas phase cooling device, the cooled cold solution and saturated damp and hot air are subjected to heat exchange in the gas phase cooling device to finish energy transfer from a gas phase to a liquid phase, the heated and heated cold solution enters a solution heating device to supplement heat required by a solution heating process, then the cold solution enters an evaporation tower for circulation, the cold air B with the reduced temperature enters an air circulation device, and condensed water obtained by cooling and condensation enters a collection system;
d. an air circulation process: the cold air B is converted into cold air A by recovering the heat of the system to the maximum extent through an air circulating device, and then enters an evaporation tower for circulation;
e. a discharging procedure: when the concentration ratio of the concentrated solution in the evaporation tower reaches a set range, the discharge pump is started to discharge the concentrated solution out of the system.
4. The evaporation process of the low-temperature normal-pressure evaporation device according to claim 3, wherein: in the step a, the heating temperature of the original solution is set to be 40-90 ℃.
5. The evaporation process of the low-temperature normal-pressure evaporation device according to claim 3, wherein: in the step b, the heated hot solution is uniformly dispersed on the filler (4) through a spray gun (5), and the spraying density is set to be 5-15m3/m2H, setting the temperature of cold air A entering the evaporation tower (2) to be 20-60 ℃, setting the circulation speed of the cold air A to be 0.5-5m/s, and directly contacting the cold air A and the hot solution on the surface of the micro-droplets to finish the mass and heat transfer process.
6. The evaporation process of the low-temperature normal-pressure evaporation device according to claim 3, wherein: in the step c, cold solution enters a first heat exchanger (14) through a circulating pump (13), circulates between the first heat exchanger (14) and a second heat exchanger (9), saturated damp and hot air enters the first heat exchanger (14) through the second heat exchanger (9), circulates between the first heat exchanger (9) and the second heat exchanger (14), heat exchange is carried out between the circulating cold solution and the saturated damp and hot air in the first heat exchanger (14), and the saturated damp and hot air after heat exchange is converted into damp and hot air; heat is transferred to the second heat exchanger (9) by the hot working medium through the working medium buffer pump (11) and the working medium pump (12), the cold solution and the hot working medium carry out secondary heat transfer in the second heat exchanger (9), the cold solution heated and heated by the first heat exchanger (14) and the second heat exchanger (9) enters the fifth heat exchanger (3), heat required by the solution heating process is supplemented, and then the cold solution enters the evaporation tower (2) for circulation; the damp and hot air enters the third heat exchanger (8) from the heat source outlet of the second heat exchanger (9), meanwhile, the cold medium enters from the cold source inlet, the rising damp and hot air exchanges heat with the cold medium, the cooled damp and hot air is condensed to form condensed water and is converted into cold air B, and the cold medium absorbs heat and enters the fourth heat exchanger (7).
7. The evaporation process of the low-temperature normal-pressure evaporation device according to claim 3, wherein: and d, enabling the cold air B to enter a fourth heat exchanger (7) to exchange heat with a cold medium absorbing heat by the third heat exchanger, converting the heat absorbed by the cold air B into cold air A, pushing the cold air A into an evaporation tower (2) through a circulating fan (6) to circulate as a separation working medium, and discharging the cold medium from a heat source outlet of the fourth heat exchanger (7).
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