CN102512835B - Multi-effect plate type rising film countercurrent evaporation concentration device and method thereof - Google Patents

Multi-effect plate type rising film countercurrent evaporation concentration device and method thereof Download PDF

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Publication number
CN102512835B
CN102512835B CN201110442494.5A CN201110442494A CN102512835B CN 102512835 B CN102512835 B CN 102512835B CN 201110442494 A CN201110442494 A CN 201110442494A CN 102512835 B CN102512835 B CN 102512835B
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plate type
heat exchanger
steam
tank
effect
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CN201110442494.5A
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CN102512835A (en
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周轶松
周鼎
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上海缔森能源技术有限公司
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Abstract

The present invention relates to the technical fields of a multi-effect evaporation concentration process and equipment, and specifically to a multi-effect plate type rising film countercurrent evaporation concentration device and a method thereof. The device comprises a plate type heat exchanger structure and a flash evaporation tank structure. The device is characterized in that the device comprises five groups of plate type rising film countercurrent evaporation devices, wherein the five groups of the plate type rising film countercurrent evaporation devices form a series connection; each group of the plate type rising film countercurrent evaporation device comprises a plate type heat exchanger, a flash evaporation tank, and a pump; each group of the plate type rising film countercurrent evaporation device is in the sealed negative pressure system condition; the pressure inside each group of the device is increased along with the increase of the raw material liquid concentration. The raw materials are subjected to heat exchange through the plate type heat exchanger, and then are separated from the solvent through the flash evaporation separator. The heat exchange treatments are sequentially performed until the material enters the fifth group of the flash evaporation tank. The heat-exchanged steam and the steam discharged from the outlet of the fifth group of the flash evaporation tank are introduced into the outlet pipe. With the present invention, the heat energy of the secondary steam after separation is completely utilized; the reverse heat exchange of the heat exchanger and the designed negative pressure and temperature condition limit the generation of the vaporization phenomenon of the material liquid in the heating process so as to reduce the scaling possibility.

Description

A kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility and method

[technical field]

The present invention relates to multiple-effect evaporation concentration technology and equipment technical field, specifically a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility and method.

[background technology]

At present, evaporating and concentrating process generally adopts shell-and-tube heat exchanger or plate type heat exchanger, and shell-and-tube heat exchanger is because it is bulky: package unit height is from two of tens meters to tens meters needs and above operating platform; Be restricted in many aspects: as requirement of material physical property, process conditions etc.So most shell-and-tube heat exchangers generally can only be accomplished triple effect design, heat exchange efficiency is too low, and therefore plate type heat exchanger replaces gradually.

Domestic patent CN1864783A discloses a kind of multi-effect distilling method for desalt and condensation and device is and the immediate domestic prior art of the present invention, a kind of multiple-effect is provided in open file, and has carried out step by step the technique of evaporation and concentration, this process using the object of countercurrent flow be the crystallization reducing in heat transfer process, but, this design does not have the step of flash separation in multiple-effect heat transfer process, in heat exchanger, can there are a large amount of vaporization phenomenons, can cause great damage to equipment, in addition, can reduce intensification thickening efficiency.In addition, its equipment has adopted plate type heat exchanger, yet but less than the heat exchanger plates to wherein, carries out concrete design, lacks flashing apparatus, under normal pressure, concentrates, and all can cause very large impact to concentration technology.

[summary of the invention]

The phenomenon that the object of the invention is to solve in prior art easy crystallization when concentrated heat-sensitive substance, provides a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility and method.

Design for achieving the above object a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility, comprise plate type heat exchanger structure, flash tank structure, it is characterized in that comprising the plate type rising film counter flow evaporation plant of five groups of series connection, every group of plate type rising film counter flow evaporation plant comprises a plate type heat exchanger, a flash tank, a pump, connecting pipe between the medium channel outlet of plate type heat exchanger and the import of flash tank, the steam channel outlet of plate type heat exchanger connects steam (vapor) outlet pipeline

Second group to the 5th group: connecting pipe between the plate type heat exchanger medium channel import of connecting pipe between the outlet of flash tank bottom and pump inlet, pump discharge and upper a group, after steam (vapor) outlet pipeline gathers with between vacuum tank import, be connected steam (vapor) outlet pipeline, connecting pipe between vacuum tank outlet and vavuum pump import;

First group to the 4th group: connecting pipe between the plate type heat exchanger steam channel import of the roof door of flash tank and its next group;

First group: the steam channel import of plate type heat exchanger is connected with extraneous jet chimney, the outlet at bottom of flash tank connects discharge pipe;

The 5th group: between the roof door of flash tank and plate-type condenser import, be connected steam (vapor) outlet pipeline, connecting pipe between plate-type condenser outlet and vacuum tank import, the feed pipe of described material liquid is connected with the medium channel import of plate type heat exchanger;

Plate type heat exchanger in first group is an effect plate type heat exchanger, plate type heat exchanger in second group is two effect plate type heat exchangers, plate type heat exchanger in the 3rd group is triple effect plate type heat exchanger, plate type heat exchanger in the 4th group is quadruple effect plate type heat exchanger, and the plate type heat exchanger in the 5th group is five effect plate type heat exchangers.

Described baffle heater heat exchanger channels draw ratio is 156~170, heat exchanger plates is herringbone corrugated plating, 30 ° of ripple angles, ripple's depth 3.85mm, normal pitch 12.6mm, effective heating intensity 1200mm, steam angle bore dia 200mm, steam (vapor) outlet diameter is 200mm.

Described flash tank, import is at 1/3rd places of tank body height overall at the bottom of tank, at tank body inner top, barrier type liquid foam catcher is set, tank body inner bottom part is provided with liquid level sensor, and described liquid level sensor monitoring liquid level is controlled at tank body height overall 300~900mm place at the bottom of tank.

Can heat exchangers in series between described extraneous jet chimney and an effect plate type heat exchanger, can heat exchangers in series on the 5th group of described tank connected steam (vapor) outlet pipeline of flash distillation.

Described feed pipe and five effects one or more heat exchangers of can connecting between plate type heat exchangers, the steam channel of heat exchanger and described one or more steam (vapor) outlet pipeline of first group to the 5th group are connected in series.

The buffer tank of can connecting on described discharge pipe, buffer tank outlet at bottom connects pump.

One or more in valve, thermometric instrument, manometer can be set on described pipeline.

The present invention also comprises a kind of Multi-effect plate type rising film countercurrent evaporation method for concentration, it is characterized in that each the group device in the method is all under airtight negative pressure system condition, absolute pressure is between 0.005Mpa~0.06MPa, control declines in gradient from first group to the 5th group equipment vacuum degree evaporating temperature that raises in gradient, control liquid level at flash tank height overall 300~600mm place at the bottom of tank

Raw material is through five effect plate type heat exchanger heat exchange, and then carry out separated through flash separator with solvent, through separated raw material, enter quadruple effect plate type heat exchanger, as said method stage-by-stage heat exchange evaporation and concentration until the 5th group of flash tank, each through 2~9 ℃ of plate-type heat-exchange actuator temperature risings, from the flash tank outlet at bottom of first group, produce concentrate; The steam trend that heat exchange is used is contrary with raw material trend, the heat steam that comes from the outside of one effect heat exchanger, raw material is flash separation after Steam Heating, steam enters two effect plate type heat exchangers and raw material heat exchange from flash drum overhead, so stage-by-stage heat exchange is until the flash tank of the 5th group, through first group to the 4th group steam of heat exchange and the steam of the 5th group of flash drum overhead outlet, enter vacuum tank, vacuum tank connects vavuum pump and vacuumizes.

The initial temperature of described charging is 45 ℃, lower than the employing electrical heating of 45 ℃, is preheated to 45 ℃.

In described method, by adding in pipeline, butterfly valve solves because the solute that vaporization produces is separated out phenomenon.

Described control is the flow that regulates heat exchanger exit steam from first group of method to the 5th group of equipment vacuum degree.

The present invention compared with the existing technology, take full advantage of the heat energy of separated rear indirect steam, reduced the energy consumption of equipment, the vaporization phenomenon (vapor-liquid separation) that the reverse heat-exchange of heat exchanger and the negative pressure of design and temperature conditions restriction feed liquid produce in heating process, greatly reduce or avoided heat exchanger plates surface scale may, the method that the pressure in the equipment in equipment improves along with the raising of material concentration has solved in common process gluconic acid sodium salt problem of crystallization very easily in concentration process.

[accompanying drawing explanation]

Fig. 1 is the equipment flowsheet of the embodiment of the present invention;

In figure: 1. an effect plate type heat exchanger 2,4,6,8,10 is extraneous steam inlet 12. material liquid import 13. vavuum pump 14. vacuum tank 15. buffer tank 16. discharge pipes of flash tank 3. 2 effect plate type heat exchanger 5. triple effect plate type heat exchanger 7. quadruple effect plate type heat exchanger 9. 5 effect plate type heat exchanger 11..

[specific embodiment]

The present invention will be further described by reference to the accompanying drawings, and the manufacturing technology of this device is very clearly concerning this professional people.

For the material stoste that need to adopt hot method evaporation and concentration: organic solution, inorganic solution, gluconic acid sodium salt (lactone) solution, steel plant wastewater are concentrated, concentrate, desalinization etc. before fruit juice, dairy products, zymotic fluid, brine waste, industrial wastewater, toxic liquid waste incineration.

Conventionally in raw material liquid, solutes content is less, takes out moisture and reaches the concentration solute liquid object that concentration extraction is high, otherwise or from solution, isolate solute and obtain required distilled water by evaporation.

Technological process:

Each group device is all under airtight negative pressure system condition, absolute pressure is between 0.005Mpa~0.06MPa, control declines in gradient from first group to the 5th group equipment vacuum degree evaporating temperature that raises in gradient, controls liquid level at flash tank height overall 300~600mm place at the bottom of tank.Wherein:

Raw material liq flow process:

Rare raw material feed liquid is inputted by outside, and------five imitate flash tanks, and---circulating pump------------------------------------an effect flash tank is exported an effect plate type heat exchanger circulating pump two effect flash tanks two effect plate type heat exchangers circulating pump triple effect flash tank triple effect plate type heat exchanger circulating pump quadruple effect flash tank quadruple effect plate type heat exchanger by rear pump---output---finished product materials to enter five effect plate type heat exchangers

Heating steam flow process:

Raw steam (Boiler Steam)---enters the first effect plate type heat exchanger and---enters the first effect flash tank and generate indirect steam and---enter the second effect plate type heat exchanger and---enter the second effect flash tank and generate indirect steam and---enter triple effect plate type heat exchanger and---enter triple effect flash tank and generate indirect steam and---enter quadruple effect plate type heat exchanger and---enter quadruple effect flash tank and generate indirect steam that------entering the 5th effect flash tank generates indirect steam---------condensate pump---discharges to enter Vacuum Balance tank to enter the cooling generation condensed water of plate-type condenser to enter the 5th effect plate type heat exchanger.

Embodiment 1:

Gluconic acid sodium salt stoste is concentrated: 45 degrees Celsius of temperature, Baume degrees 16, the five effect unit vacuum absolute pressure 0.0123MPa when the mother liquor that oxidizing process generates enters this unit the 5th effect, 50 degrees Celsius of evaporating temperatures; While entering quadruple effect evaporation element after dehydration by evaporation, mother liquor temperature is that 50 degrees Celsius, Baume degrees bring up to approximately 18~19, quadruple effect unit vacuum absolute pressure 0.018MPa, 57 degrees Celsius of evaporating temperatures; While entering triple effect evaporation unit after dehydration by evaporation, mother liquor temperature is that 57 degrees Celsius, Baume degrees are brought up to approximately 21, the triple effect unit vacuum absolute pressure 0.024MPa, 64 degrees Celsius of evaporating temperatures; While entering the second effect evaporation element after dehydration by evaporation, mother liquor temperature is that 64 degrees Celsius, Baume degrees are brought up to approximately 24, the second effect unit vacuum absolute pressure 0.033MPa, 72 degrees Celsius of evaporating temperatures; While entering the first effect evaporation element after dehydration by evaporation, mother liquor temperature is that 72 degrees Celsius, Baume degrees are brought up to approximately 27, the first effect unit vacuum absolute pressures 0.047,80 degrees Celsius of evaporating temperatures; The mother liquor Baume degrees that the first effect vacuum separation goes out brings up to approximately 30,80 degrees Celsius of temperature, and concentration is about 80%, and the parameter that has reached finished fluid is exported by positive displacement pump.

Embodiment 2:

Gluconolactone stoste is concentrated: original concentration approximately 17% when the mother liquor that fermentation method generates enters this unit, temperature is about 30~35 degrees Celsius, through entering the 5th effect as plate-type condenser, the condensed water heat exchanger temperature after heating of series connection are promoted to 40 degrees Celsius of the moons, the 5th effect unit vacuum absolute pressure is controlled at 0.01MPa, 46 degrees Celsius of evaporating temperatures; While entering quadruple effect evaporation element after dehydration by evaporation, mother liquor temperature is 46 degrees Celsius, quadruple effect unit vacuum absolute pressure 0.015MPa, 53 degrees Celsius of evaporating temperatures; While entering triple effect evaporation unit after dehydration by evaporation, mother liquor temperature is 53 degrees Celsius, triple effect unit vacuum absolute pressure 0.02MPa, 60 degrees Celsius of evaporating temperatures; While entering the second effect evaporation element after dehydration by evaporation, mother liquor temperature is 60 degrees Celsius, the second effect unit vacuum absolute pressure 0.03MPa, 69 degrees Celsius of evaporating temperatures; While entering the first effect evaporation element after dehydration by evaporation, mother liquor temperature is 69 degrees Celsius, the first effect unit vacuum absolute pressure 0.04,75 degrees Celsius of evaporating temperatures; The mother liquid concentration that the first effect vacuum separation goes out brings up to approximately 70~80%, 75 degrees Celsius of temperature, and the parameter that has reached finished fluid is exported by positive displacement pump.

Main points:

(1) to take to rise film reverse-flow for plate type heat exchanger flow process, and heat transfer coefficient is higher, uniform distribution of temperature field, and cloth liquid is even, there will not be dry plate phenomenon.Plate type heat exchanger heat exchanger channels the Best Size Ratio is between 156~170.

(2) through the heat exchanger plates technical parameter of selecting after assay optimization many times, be: herringbone corrugated, angle 130 degree, degree of depth 3.85mm, normal pitch 12.6mm, the effective heated length 1200mm of heating plate face, material is stainless 316L, steam angle bore dia 200mm.

(3) plate type heat exchanger indirect steam outlet diameter 200mm, butterfly valve is housed as choke valve purposes, regulate material liquid to be subject to the pressure differential of thermal process and indirect steam outlet, control material liquid at the pressure of heating process, make it not occur to produce because of vaporization solute and separate out phenomenon, avoid occurring forming because of solute implantation heat exchanger plates surface the adverse consequences that fouling causes heat exchange efficiency decline and even equipment failure.

(4) plate type heat exchanger mother liquor outlet takes level to connect with flash tank, enters the position of flash tank height for upwards dividing for the total Senior Three of tank body from pot bottom, and outside tank body, garden tangent line enters.Upper space guarantees the required enough dischargeable capacitys of vapor-liquid separation, and in gas outlet, top, is provided with grating type liquid foam trap, and bottom liquid storage height should be controlled at 300~600mm automatically by liquid level sensor.

(5) material liquid and heating source adverse current be except having improved the advantages such as heat transfer efficiency, because material liquid is along with the raising temperature of concentration also corresponding raising process has solved in common process gluconic acid sodium salt in a concentration process difficult problem for crystallization very easily.

Heating steam technical process: 105~110 degrees Celsius of saturated vapor (boiler generation) temperature enter the first effect plate type heat exchanger as thermal source and add hot mother liquor and generate approximately 80 degrees Celsius of indirect steam temperature via flash tank and enter the second effect evaporation element as thermal source, and the second effect mother liquor is heated and generates indirect steam and removes to heat triple effect mother liquor.Same process, successively until the 5th effect evaporation element.The indirect steam temperature degree Celsius of each effect is: the first 80 degrees Celsius of effects, the second 72 degrees Celsius of effects, 64 degrees Celsius of triple effects, 57 degrees Celsius of quadruple effects, the 5th 50 degrees Celsius of effects.The indirect steam that the 5th effect generates enters plate-type condenser and is cooled to condensed water and enters Vacuum Balance tank and collect, by condensate pump vacuum breaker removal system.The first effect to the condensed water of quadruple effect collects by being discharged by condensate pump by entering Vacuum Balance tank after plate type heat exchanger preheating material liquid.

Principle:

This installs all heating, evaporation, condensation process process and all under closed system condition, carries out, and the fluctuations of vacuum that causes affecting technological operation is unallowed, during Design and manufacture, has also fully taken into account these problems.

Need concentrated raw material liq by outside, by pipeline, to be entered the 5th effect heater (plate type heat exchanger) of this unit, feed liquid is taken over and is entered heater from bottom, by can be with the form that rises film flowing from bottom to top at a high speed in passage between heating plates after opposite side thermal source steam indirect, the motive force of working fluid comes from the lift being produced by the temperature difference after liquid is heated, in heat exchanger runner, raw material liq absorbs after enough heat energy moment and departs from heater and with liquid form, enter the 5th effect flash tank and under the effect of gravity, be separated into two-phase fluid (in flash tank, absolute pressure is less than the pressure in heater runner), what rise is that (the 5th effect is that last effect steam of this unit no longer enters next effect as thermal source to steam component, other each effect enters the heater of next effect) enter plate type heat exchanger and be condensed into water and converge and enter Vacuum Balance tank and have the condensate pump continuous wave output of dividing into.The bottom entrance that the circulating pump that the feed liquid of the 5th effect flash tank separate and subside arranges via bottom is transported to quadruple effect heater being heated from bottom to top, feed liquid rises film and enters quadruple effect flash tank and be separated into two-phase fluid (in tank with heater have pressure reduction) after heater is heated, and same steam component departs from tank body and enters next effect heater (the 5th effect) removes to heat opposite side in this effect heater material as thermal source.In like manner, it is like this for the process water between other each effect.Each is imitated steam and after passing out energy, has also reduced the temperature of self and be phase-changed into condensed water through the condensing water conduit output of the bottom of each effect heater hot side, and each heater cold water output channel is recycled after state (vacuum is produced by vacuum pump system) the lower link gathering tube of negative pressure enters Vacuum Balance tank.And the feed liquid for higher than rear one-level concentration of the heavy phase that enters flash tank to be liquid decline precipitation enters upper level heater again and accepts heating.As the steam of heat source by last effect backward an effect flow, material liquid is flowed to last effect by a rear effect, each imitates process more than repetition continuous and constant basis.Owing to having presetted pressure and temperature process conditions in heater, so having controlled feed liquid produces and occurs vaporization phenomenon (vapor-liquid separation) in heating process, select heat-exchanger ripple plate structure parameter to be conducive to surperficial self-cleaning, so greatly reduce or avoided heat exchanger plates surface scale possible simultaneously.The thermal source of the first effect heater is from external steam or other thermals source, and other thermal source of respectively imitating heater to be isolated steam by previous stage flash tank provide, so realized a thermal source and repeatedly utilized and reached energy-conservation object.The heat energy that N effect consumes is in theory 1/N, according to design of the present invention can accomplish 5~10 effect and more than, effect number is more much more energy-conservation, and < < multiple-effect package > > etc. can accomplish that 3 effects are also difficult under identical material and process conditions, so only according to effect mathematics opinion, infer, efficiency of the present invention method has than before improved several times.。The separated steam producing of last effect enters plate-type condenser and is condensed into liquids recovery.Thermal source steam is from a front effect effect process backward, and feed liquid is to be advanced to last effect by a rear effect.

The vacuum of system is generated in advance by water ring vacuum pump, in the closed system having generated, each effect brings into operation, when imitating heat exchanger to last effect heating steam condensation by each, vacuum during work clasps, the stable of evaporating temperature determined in the control of vacuum, guarantees the completeness that flash tank vapour-liquid is discrete simultaneously.

By each effect, dodge separated steaming pot bottom material automatic Control Systems of Liquids Height, the balance distribution that can guarantee respectively to imitate the equilibrium heating of heater and then guarantee respectively to imitate evaporation capacity.

Five effect plate type rising film adverse current flash evaporation vacuum complexes: for gluconic acid sodium salt, glucolactone dilute liquid concentration technology requires to manufacture and design, the operation of passing through to concentrate at food chemistry workshop of 5 five effect plate type rising film adverse current flash vacuum techniques, evaporated water per hour is 5 tons, consume approximately 1.1 tons of steam, Energy Efficiency Ratio is 1: 4.5, and the existing equipment of same object can only be accomplished 2~3 effects, evaporate 5 tons of water and need consume 3 tons of steam, approximately 2 tons of this unit steam savings per hour, finished product requisite quality and stable, energy-saving and water-saving effect is remarkable, reduce by approximately 2/3~3/4 thermal pollution discharge capacity.

Claims (7)

1. a Multi-effect plate type rising film countercurrent evaporation enrichment facility, comprise plate type heat exchanger structure, flash tank structure, it is characterized in that comprising the plate type rising film counter flow evaporation plant of five groups of series connection, every group of plate type rising film counter flow evaporation plant comprises a plate type heat exchanger, a flash tank, a pump, connecting pipe between the medium channel outlet of plate type heat exchanger and the import of flash tank, the steam channel outlet of plate type heat exchanger connects steam (vapor) outlet pipeline
Second group to the 5th group: connecting pipe between the plate type heat exchanger medium channel import of connecting pipe between the outlet of flash tank bottom and pump inlet, pump discharge and upper a group, after steam (vapor) outlet pipeline gathers with between vacuum tank import, be connected steam (vapor) outlet pipeline, connecting pipe between vacuum tank outlet and vavuum pump import;
First group to the 4th group: connecting pipe between the plate type heat exchanger steam channel import of the roof door of flash tank and its next group;
First group: the steam channel import of plate type heat exchanger is connected with extraneous jet chimney, the outlet at bottom of flash tank connects discharge pipe;
The 5th group: between the roof door of flash tank and plate-type condenser import, be connected steam (vapor) outlet pipeline, connecting pipe between plate-type condenser outlet and vacuum tank import, the feed pipe of described material liquid is connected with the medium channel import of plate type heat exchanger;
Plate type heat exchanger in first group is an effect plate type heat exchanger, plate type heat exchanger in second group is two effect plate type heat exchangers, plate type heat exchanger in the 3rd group is triple effect plate type heat exchanger, plate type heat exchanger in the 4th group is quadruple effect plate type heat exchanger, and the plate type heat exchanger in the 5th group is five effect plate type heat exchangers;
Described plate type heat exchanger heat exchanger channels draw ratio is 156~170, heat exchanger plates is herringbone corrugated plating, 30 ° of ripple angles, ripple's depth 3.85mm, normal pitch 12.6mm, effective heating intensity 1200mm, steam angle bore dia 200mm, steam (vapor) outlet diameter is 200mm;
Described flash tank, import is at 1/3rd places of tank body height overall at the bottom of tank, at tank body inner top, barrier type liquid foam catcher is set, tank body inner bottom part is provided with liquid level sensor, and described liquid level sensor monitoring liquid level is controlled at tank body height overall 300~600mm place at the bottom of tank;
The film countercurrent evaporation method for concentration that rises of described Multi-effect plate type rising film countercurrent evaporation enrichment facility is: each the group device in the method is all under airtight negative pressure system condition, absolute pressure is between 0.005Mpa~0.06MPa, control declines in gradient from first group to the 5th group equipment vacuum degree evaporating temperature that raises in gradient, control liquid level at flash tank height overall 300~600mm place at the bottom of tank, raw material is through five effect plate type heat exchanger heat exchange, and then carry out separated through flash separator with solvent, through separated raw material, enter quadruple effect plate type heat exchanger, as said method stage-by-stage heat exchange evaporation and concentration until first group of flash tank, each through 2~9 ℃ of plate-type heat-exchange actuator temperature risings, from the flash tank outlet at bottom of first group, produce concentrate, the steam trend that heat exchange is used is contrary with raw material trend, the heat steam that comes from the outside of one effect heat exchanger, raw material is flash separation after Steam Heating, steam enters two effect plate type heat exchangers and raw material heat exchange from flash drum overhead, so stage-by-stage heat exchange is until the flash tank of the 5th group, through first group to the 4th group steam of heat exchange and the steam of the 5th group of flash drum overhead outlet, enter vacuum tank, vacuum tank connects vavuum pump and vacuumizes.
2. a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility as claimed in claim 1, is characterized in that heat exchangers in series between described extraneous jet chimney and an effect plate type heat exchanger, heat exchangers in series on the 5th group of described tank connected steam (vapor) outlet pipeline of flash distillation.
3. a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility as claimed in claim 1, it is characterized in that described feed pipe and five imitates one or more heat exchangers of connecting between plate type heat exchangers, the steam channel of heat exchanger and described one or more steam (vapor) outlet pipeline of first group to the 5th group are connected in series.
4. a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility as claimed in claim 1, the buffer tank that it is characterized in that connecting on described discharge pipe, buffer tank outlet at bottom connects pump.
5. as the Multi-effect plate type rising film countercurrent evaporation enrichment facility as described in arbitrary in claim 1~4, it is characterized in that arranging one or more in valve, thermometric instrument, manometer on described pipeline.
6. a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility as claimed in claim 1, is characterized in that in film countercurrent evaporation method for concentration, butterfly valve solves because the solute that vaporization produces is separated out phenomenon by adding in pipeline in described rising.
7. a kind of Multi-effect plate type rising film countercurrent evaporation enrichment facility as claimed in claim 1, is characterized in that the initial temperature of described charging is 45 ℃, lower than the employing electrical heating of 45 ℃, is preheated to 45 ℃.
CN201110442494.5A 2011-12-26 2011-12-26 Multi-effect plate type rising film countercurrent evaporation concentration device and method thereof CN102512835B (en)

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Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0593687B1 (en) * 1991-11-23 1997-05-14 Geysir Ag Process and device for the desalination of sea water using a plate type heat exchanger
CN101229449A (en) * 2007-10-31 2008-07-30 大连理工大学 Pleietrepie counter current falling film evaporator of organic solvent recycle
CN101289384A (en) * 2008-04-28 2008-10-22 河南金丹乳酸有限公司 Use method of multiple-effect falling film concentrating device in production of lactic acid
CN201492956U (en) * 2009-09-01 2010-06-02 兆光生物工程(邹平)有限公司 Sextuple-effect eight-body falling film evaporation system
CN202366490U (en) * 2011-12-26 2012-08-08 上海缔森能源技术有限公司 Multi-effect evaporation and concentration device

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0593687B1 (en) * 1991-11-23 1997-05-14 Geysir Ag Process and device for the desalination of sea water using a plate type heat exchanger
CN101229449A (en) * 2007-10-31 2008-07-30 大连理工大学 Pleietrepie counter current falling film evaporator of organic solvent recycle
CN101289384A (en) * 2008-04-28 2008-10-22 河南金丹乳酸有限公司 Use method of multiple-effect falling film concentrating device in production of lactic acid
CN201492956U (en) * 2009-09-01 2010-06-02 兆光生物工程(邹平)有限公司 Sextuple-effect eight-body falling film evaporation system
CN202366490U (en) * 2011-12-26 2012-08-08 上海缔森能源技术有限公司 Multi-effect evaporation and concentration device

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