CN110197703A - A kind of flash distillation rate calculations method of flash process in alumina evaporation process - Google Patents
A kind of flash distillation rate calculations method of flash process in alumina evaporation process Download PDFInfo
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- CN110197703A CN110197703A CN201910499489.4A CN201910499489A CN110197703A CN 110197703 A CN110197703 A CN 110197703A CN 201910499489 A CN201910499489 A CN 201910499489A CN 110197703 A CN110197703 A CN 110197703A
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Abstract
The present invention provides a kind of flash distillation rate calculations method of flash process in alumina evaporation process, is related to industry automatic control applied technical field.Steps are as follows by the present invention: step 1: obtaining alumina evaporation system real process data；Step 2: judging the inlet amount of flash system whether in normal working range 450m3/ hour~650m3/ hour if so, going to step 3；If it is not, thening follow the steps 1；Step 3: the boiling point that the data according to obtained in step 1 obtain sodium aluminate solution rises △ 'BPE；Step 4: △ ' is risen according to the boiling point that step 3 obtainsBPEFlash distillation rate CFS is calculated, according to the intensity of the practical alumina producing flash distillation of the online Real-Time Evaluation of obtained CFS.The flash distillation intensity of on-line evaluation flash vessel of the present invention improves the evaporation effect of evaporation process, energy-saving is of great significance to instructing alumina evaporation to produce.
Description
Technical field
The present invention relates to flashed in industry automatic control applied technical field more particularly to a kind of alumina evaporation process
The flash distillation rate calculations method of journey.
Background technique
Evaporation is an important process in process for making alumina, and task is to evaporate water extra in mother liquor,
Improve circulating mother liquor concentration.However the steam consumption of evaporator occupies very big specific gravity in aluminum oxide production process, in order to reduce
Steam consumption for evaporation, reduces production cost, and domestic alumina producer generallys use six effect tube type falling-film evaporations of high-efficiency low energy consumption at this stage
The thermal efficiency can be improved additionally by stoste flash evaporation technology is introduced in the evaporation technique that device is combined with flash vessel, reduces steam and disappears
Consumption.In practical alumina evaporation production process, mainly with the whether qualified evaluation evaporation effect of circulating mother liquor concentration, to steam water
The indexs such as amount, steam-water ratio evaluate steam consumption.These evaluation indexes are from the entire evaporation process evaporation effect of macroscopically evaluation
Fruit is not concerned with single evaporator evaporation effect, and is all off-line calculation, without real-time.Due to the flash distillation of evaporation process
The flash evaporation effect of device will directly affect the production effect of entire alumina evaporation process, but in actual production process and not know
The flash distillation intensity of each individual flash vessel of road, therefore analysis is carried out by the single flash vessel to alumina evaporation process and is ground
Study carefully, the flash distillation intensity of Utilization assessment index on-line evaluation flash vessel, it is important to instructing alumina producing, raising flash efficiency to have
Meaning.
Summary of the invention
The technical problem to be solved by the present invention is in view of the above shortcomings of the prior art, provide a kind of alumina evaporation process
The flash distillation rate calculations method of middle flash process, the flash distillation intensity of on-line evaluation flash vessel of the present invention, to instructing alumina evaporation
Production improves the evaporation effect of evaporation process, energy-saving is of great significance.
In order to solve the above technical problems, the technical solution used in the present invention is:
The present invention provides a kind of flash distillation rate calculations method of flash process in alumina evaporation process, including walks as follows
It is rapid:
Step 1: obtaining alumina evaporation system real process data；
Process data in acquisition alumina evaporation process flash system in real time, the data include: current stoste flash distillation
The input concentration of device, feeding temperature, feed rate, drop temperature, flash vessel inner equilibrium pressure, secondary steam temperature；
Step 2: judging the inlet amount of flash system whether in normal working range 450m3/ hour~650m3/ hour?
If so, going to step 3；If it is not, thening follow the steps 1；
Step 3: the boiling point that the data according to obtained in step 1 obtain sodium aluminate solution rises △ 'BPE；
Step 3.1: calculating corresponding saturation temperature under the pressure currently obtained；
Current flash vessel inner equilibrium pressure p is switched into engineering pressure P under absolute pressure, unit is kg/cm2, it is shown below:
P=(p+0.101325)/0.098
Secondary steam saturation temperature TpThe relational expression between engineering pressure P corresponding thereto are as follows:
Wherein b0, b1, b2, b3, b4For parameter, the parameter is satisfied as corresponding to saturated vapour pressure under current production status
It is obtained with the data in the temperature table of comparisons by the practical fitting of least square method；
Step 3.2: calculating the boiling point liter under sodium aluminate solution normal pressure；
The boiling point liter of sodium aluminate solution is related with the concentration in solution containing alkali and current solution temperature, in alumina producing
Evaporization process in, boiling point under sodium aluminate solution normal pressure rises △BPERelational expression are as follows:
△BPE=c0+c1Nk+c2Tin+c3NkTin+c4Nk2+c5Tin 2+c6NkTin 2+c7Nk2Tin+c8Nk3+c9Tin 3
Wherein c0, c1, c2, c3, c4, c5, c6, c7, c8, c9For parameter, the parameter is that basis goes out under current production status
Sodium aluminate solution concentration at material mouth obtain after production carries out polynomial regression fit to above formula with the data chemically examined,
Nk is caustic alkali concentration, TinFor feedstock solution temperature；
Step 3.3: △ is risen to boiling point according to Ji Xinke formulaBPEIt is modified, obtains revised boiling point and rise △ 'BPE；
Since the pressure change of solution will lead to the variation of feed liquid boiling point, according to Ji Xinke formula under sodium aluminate solution normal pressure
The elevation of boiling point be corrected, formula are as follows:
△′BPE=f △BPE
Wherein f is correction coefficient, its calculation formula is:
Wherein r be current production status pressure under secondary steam the latent heat of vaporization；
By carrying out regression analysis to vapor (steam) temperature and heat content table, the relational expression of steam latent heat and temperature is obtained are as follows:
R=d1-d2Tp-d3Tp 2
Wherein d1, d2, d3For parameter, the data in vapor (steam) temperature and heat content table are returned according under current production status
Fitting is returned to obtain；
The boiling point that can be calculated revised sodium aluminate solution by calculating above-mentioned steps rises △ 'BPE:
Step 4: △ ' is risen according to the boiling point that step 3 obtainsBPEFlash distillation rate CFS is calculated, it is real-time online according to obtained CFS
The intensity flashed in practical aluminum oxide production process is evaluated, is shown below:
Wherein TinFor feedstock solution temperature, ToutFor the solution temperature that discharges, TsatFor the saturation under pressure corresponding with solution
Temperature, Tsat=Tp+△′BPE；τ is residence time of the solution in flash vessel,Q is feed rate, and α is flash vessel
Radius, h are liquid level in flash vessel.
The beneficial effects of adopting the technical scheme are that in a kind of alumina evaporation process provided by the invention
The flash distillation rate calculations method of flash process, the online process data provided using computer system and conventional detection instrument,
It is combined by the calculation method for rising sodium aluminate solution boiling point in flash process with the calculation method of flash distillation rate, by not
With the charging degree of superheat, feed rate carries out calculating analysis to the index under flash vessel liquid level, equilibrium pressure condition, ties
Fruit shows that we can use the intensity of the flash distillation online Real-Time Evaluation of this index of rate practical alumina producing flash distillation, to instructing oxygen
Change aluminum evaporation production process, improves the evaporation effect of evaporation process, energy-saving is of great significance.
Detailed description of the invention
Fig. 1 is the process and schematic device in stoste flash process provided in an embodiment of the present invention circuit, wherein 1 is secondary
Vapour tension thermometer, 2 be flash vessel liquidometer, 3 be drop temperature meter, 4 be flash vessel pressure gauge, 5 be feeding temperature meter, 6 for into
Stream meter, 7 be stoste flash vessel, and 8 be input concentration meter；
Fig. 2 is flash distillation rate CFS calculation flow chart provided in an embodiment of the present invention；
Fig. 3 is flash distillation rate CFS provided in an embodiment of the present invention in input concentration, pressure, liquid level and feeding flow
With the variation diagram of the degree of superheat when amount is held essentially constant；
Fig. 4 is that flash distillation rate CFS provided in an embodiment of the present invention is basic in input concentration, the degree of superheat and feed rate
With the variation diagram of liquid level when remaining unchanged；
Fig. 5 is flash distillation rate CFS provided in an embodiment of the present invention in input concentration, liquid level, the degree of superheat and charging
With the variation diagram of pressure when flow is held essentially constant；
Fig. 6 is flash distillation rate CFS provided in an embodiment of the present invention in input concentration, liquid level, the degree of superheat and pressure
With the variation diagram of feed rate when being held essentially constant；
Fig. 7 is flash distillation rate CFS provided in an embodiment of the present invention in feed rate, liquid level, the degree of superheat and pressure
With the variation diagram of input concentration when being held essentially constant.
Specific embodiment
With reference to the accompanying drawings and examples, specific embodiments of the present invention will be described in further detail.Implement below
Example is not intended to limit the scope of the invention for illustrating the present invention.
The index Evaluation Method of alumina evaporation process flash system of the invention depends on flash system hardware platform, by
The software program write realizes that the program is used to acquire input concentration, feeding temperature, the feeding flow of current stoste flash vessel
Amount, drop temperature, flash vessel inner equilibrium pressure, the data such as secondary steam temperature.
Its hardware platform core is made of stoste flash vessel and relevant device, while being equipped with measuring instrumentss, executes machine
Structure and the computer system for carrying out software calculating.Vaporizing raw liquor enters stoste flash vessel by feed inlet and is flashed, then
Enter lower 1st effective evaporator by discharge hole for discharge to continue to evaporate, a large amount of steam can be generated in flash process, pass through flash distillation
Secondary steam outlet at the top of device continues to heat into next evaporator, as shown in Figure 1, detailed construction is as follows:
Further include following measuring instrumentss using flash vessel as the flash system of core:
Based on the feeding temperature of on-line measurement feeding temperature, it is mounted on stoste flash vessel feed inlet conduits；
For the flowmeter of on-line measurement stoste flash vessel feed rate, it is mounted on stoste flash vessel feed inlet conduits
On；
For the densimeter of on-line measurement stoste flash vessel input concentration, it is mounted on stoste flash vessel feed inlet conduits
On；
For the pressure gauge of on-line measurement secondary steam pressure, it is mounted on stoste flash vessel discharge port；
Based on the drop temperature of on-line measurement stoste flash vessel drop temperature, it is mounted on the discharge pipe of stoste flash vessel
On；
Differential pressure levelmeter is housed on stoste flash vessel, for detecting liquid level in flash vessel；
The flash system is configured with distributed computer control system (DCS) or programmable logic controller (PLC) simultaneously
(PLC) or industrial control computer (IPC) or discrete industrial regulator；Above-mentioned measuring instrumentss and executing agency are connected to control
The flash distillation rate calculations method of computer processed, alumina evaporation process of the invention both may operate in computer control system
It monitors on computer, can also run on independent optimal setting computer, which passes through (distributed with control computer
Computer control system (DCS) or programmable logic controller (PLC) (PLC) or industrial control computer (IPC)) it is communicated, it obtains
Real-time process data is obtained, and provides the calculated value of flash distillation rate.
As shown in Fig. 2, the method for the present embodiment is as described below.
The present invention provides a kind of flash distillation rate calculations method of flash process in alumina evaporation process, including walks as follows
It is rapid:
Step 1: obtaining alumina evaporation system real process data；
Data in acquisition alumina evaporation process flash system in real time, which includes: current stoste flash vessel
Input concentration, feeding temperature, feed rate, drop temperature, flash vessel inner equilibrium pressure, secondary steam temperature；
Step 2: judging the inlet amount of flash system whether in normal working range 450m3/ hour~650m3/ hour?
If so, going to step 3；If it is not, thening follow the steps 1；
Step 3: the boiling point that the data according to obtained in step 1 obtain sodium aluminate solution rises △ 'BPE；
The feed liquid elevation of boiling point refers to that under conditions of same pressure, the boiling temperature of feed liquid is higher than the boiling temperature of pure water；
In alumina evaporation production process, due to the continuous variation of feed concentration, cause feed liquid boiling point in evaporator different；While by
In there are certain pressure in evaporator, this has also resulted in the difference of feed liquid boiling point.
Since boiling point liter has an impact to the calculating of flash process index of correlation, needs substantially to calculate out-feed liquid boiling point and appreciate,
The following are main calculating steps:
Step 3.1: calculate corresponding saturation temperature under the pressure currently obtained:
Due to the secondary steam overheat in actual production, we can be by obtaining corresponding saturation temperature by steam pressure
Degree；Current flash vessel inner equilibrium pressure p is switched into engineering pressure P under absolute pressure first, unit is kg/cm2, it is shown below:
P=(p+0.101325)/0.098
Secondary steam saturation temperature TpThe relational expression between engineering pressure P corresponding thereto are as follows:
Wherein b0, b1, b2, b3, b4For parameter, the parameter is obtained by alumina evaporation process-field under current production status
The corresponding saturation temperature table of comparisons of saturated vapour pressure in data by least square method it is practical fitting obtain,
It is obtained in the present embodiment:
Tp=68 × P0.3-48011×P-0.0003+48042
Step 3.2: calculating the boiling point liter under sodium aluminate solution normal pressure；
The boiling point liter of sodium aluminate solution is related with the concentration in solution containing alkali and current solution temperature, in alumina producing
Evaporization process in, boiling point under sodium aluminate solution normal pressure rises △BPERelational expression are as follows:
△BPE=c0+c1Nk+c2Tin+c3NkTin+c4Nk2+c5Tin 2+c6NkTin 2+c7Nk2Tin+c8Nk3+c9Tin 3
Wherein c0, c1, c2, c3, c4, c5, c6, c7, c8, c9For parameter, the parameter is that basis goes out under current production status
Sodium aluminate solution concentration at material mouth obtain after production carries out polynomial regression fit to above formula with the data chemically examined,
Nk is caustic alkali concentration, TinFor feedstock solution temperature；
The present embodiment is to recognize that unknown parameter therein can be obtained to above formula by actual production and analysis data:
△BPE=1.5+0.007 × Nk+3 × 10-5×Tin+2×10-4×Nk×Tin
+1×10-4×Nk2-3.8×10-8×Tin 2+1.7×10-10×Nk×Tin 2
-2.5×10-7×Tin×Nk2-9×10-10×Nk3-8.6×10-10×Tin 3
Step 3.3: △ is risen to boiling point according to Ji Xinke formulaBPEIt is modified, obtains revised boiling point and rise △ 'BPE；
Since the pressure change of solution will lead to the variation of feed liquid boiling point, according to Ji Xinke formula under sodium aluminate solution normal pressure
The elevation of boiling point be corrected, formula are as follows:
△′BPE=f △BPE
Wherein f be correction coefficient, zero dimension, using experience calculate its calculation formula is:
The wherein latent heat of vaporization of the r for secondary steam (saturated steam) under the pressure of current production status, unit kJ/
kg；
The latent heat of vaporization of secondary steam is needed in above formula, however steam enthalpy will receive the influence of steam pressure and temperature,
For actual normal processes, the accurate mathematical relationship between steam latent heat and evaporimeter internal pressure and temperature is hardly resulted in.It is right
The macroscopic property of saturated water and saturated vapor carries out analysis and learns that influence of the variation of steam pressure to latent heat of the steam is very
It is small, its influence to steam latent heat can be ignored, and vapor (steam) temperature has large effect to steam latent heat.Thus can lead to
It crosses and regression analysis is carried out to vapor (steam) temperature and heat content table, obtain the relational expression of steam latent heat and temperature are as follows:
R=d1-d2Tp-d3Tp 2
Wherein d1, d2, d3For parameter, the data in vapor (steam) temperature and heat content table are returned according under current production status
Fitting is returned to obtain；
It can be calculated the boiling point liter △ ' of theoretical sodium aluminate solution after amendment by calculating above-mentioned stepsBPE:
Step 4: △ ' is risen according to the boiling point that step 3 obtainsBPEFlash distillation rate CFS is calculated, it is real-time online according to obtained CFS
The intensity flashed in practical aluminum oxide production process is evaluated, is shown below:
The flash distillation rate CFS of WangYu et al. definition circulation flash distillation, for indicating the intensity of flash distillation progress, such as following formula institute
Show:
Wherein TinFor feedstock solution temperature, ToutFor the solution temperature that discharges, TsatFor the saturation under pressure corresponding with solution
Temperature, Tsat=Tp+△′BPE；τ is residence time of the solution in flash vessel,Q is feed rate, and α is flash vessel
Radius, h are liquid level in flash vessel.
It is found by carrying out analysis to actual production data, flashes rate due to considering stop of the feed liquid in flash vessel
Time, so very enough more comprehensive true intensities for measuring flash distillation.
The present embodiment is the stoste flash process of an Alumina refinery.The wherein model Φ 4.8m of stoste flash vessel
×4.5m；Following measuring instrumentss are installed first, in accordance with the requirement of this method, comprising: electromagnetic flowmeter survey stoste flash vessel into
Stream amount Q；Thermometer measure original flash vessel feedstock solution temperature Tin；Thermometer measure original flash vessel discharging solution temperature Tout；Pressure
Power meter measures stoste flash vessel inner equilibrium pressure p；Nk densimeter measures stoste flash vessel input concentration；Electric control valve control is former
Liquid flash vessel feed rate；
The automatic control of computer control system (DCS) optimized integration control loop in a distributed manner uses in slave computer
Single-loop regulator configuration in DCS is at following base control circuit: original dodge feed rate electric control valve control original dodge into
Stream amount,
In host computer (monitoring computer) with Foxview software realization monitoring human-computer interface.The feeding flow of the flash system
Measure normal range of operation are as follows: original dodges feed rate --- 450m3/ hour~650m3/ hour
The calculation procedure for flashing index is worked out with the MATLAB application software that MathWorks is provided, and is individually being optimized
It is run on computer, is responsible for carrying out data communication with DCS and host computer equipped with OPC Server on the computer.
The present invention calculates the flash distillation rate of flash process using actual production data, wherein flash distillation rate CFS is in pressure, liquid
With the variation of the degree of superheat, design parameter when position height, feed rate and original liquid concentration are held essentially constant are as follows:-
77.2kPa,0.87m,572m3/ h, 177g/l, as a result as shown in Figure 3；Flash rate CFS the degree of superheat, pressure, feed rate,
And original liquid concentration when being held essentially constant with the variation of liquid level, design parameter are as follows: 1.5 DEG C, -72.5kPa, 595m3/
H, 177g/l, as a result as shown in Figure 4；It is basic in the degree of superheat, liquid level, feed rate and original liquid concentration to flash rate CFS
With the variation of pressure, design parameter when remaining unchanged are as follows: 1.5 DEG C, 0.77m, 595m3/ h, 175g/l, as a result as shown in Figure 5；
Rate CFS is flashed when the degree of superheat and pressure, liquid level, original liquid concentration are held essentially constant with the change of feed rate
Change, design parameter are as follows: 1.7 DEG C, -74.5kPa, 0.82m, 163g/l, as a result as shown in Figure 6；Flash rate CFS the degree of superheat,
With the variation of original liquid concentration, design parameter when pressure, liquid level and feed rate are held essentially constant are as follows: 1.7 DEG C ,-
74.5kPa,0.82m,586m3/ h, as a result as shown in Figure 7.It can be obtained by the analysis to result: in aluminum oxide production process,
The flash distillation rate CFS of stoste flash vessel increases with the increase of feed rate and balance pressure, with liquid membrane and charging
Concentration increases and reduces, and thus flashes the intensity that this index of rate CFS is able to reflect flash evaporation effect；In practical alumina evaporation
In production process, the calculation method that can use flash distillation rate CFS in the alumina evaporation process in the present invention is commented in real time online
The flash distillation intensity of flash vessel during valence alumina evaporation, the production to alumina evaporation process is instructed improve evaporation process
Evaporation effect energy-saving is of great significance.
Finally, it should be noted that the above embodiments are merely illustrative of the technical solutions of the present invention, rather than its limitations；Although
Present invention has been described in detail with reference to the aforementioned embodiments, those skilled in the art should understand that: it still may be used
To modify to technical solution documented by previous embodiment, or some or all of the technical features are equal
Replacement；And these are modified or replaceed, model defined by the claims in the present invention that it does not separate the essence of the corresponding technical solution
It encloses.
Claims (1)
1. a kind of flash distillation rate calculations method of flash process in alumina evaporation process, characterized by the following steps:
Step 1: obtaining alumina evaporation system real process data；
Process data in acquisition alumina evaporation process flash system in real time, which includes: current stoste flash vessel
Input concentration, feeding temperature, feed rate, drop temperature, flash vessel inner equilibrium pressure, secondary steam temperature；
Step 2: judging the inlet amount of flash system whether in normal working range 450m3/ hour~650m3/ hour? if so,
Then go to step 3；If it is not, thening follow the steps 1；
Step 3: the boiling point that the data according to obtained in step 1 obtain sodium aluminate solution rises △ 'BPE；
Step 3.1: calculating corresponding saturation temperature under the pressure currently obtained；
Current flash vessel inner equilibrium pressure p is switched into engineering pressure P under absolute pressure, unit is kg/cm2, it is shown below:
P=(p+0.101325)/0.098
Secondary steam saturation temperature TpThe relational expression between engineering pressure P corresponding thereto are as follows:
Wherein b0, b1, b2, b3, b4For parameter, parameter saturation temperature as corresponding to saturated vapour pressure under current production status
Data in the degree table of comparisons are obtained by the practical fitting of least square method；
Step 3.2: calculating the boiling point liter under sodium aluminate solution normal pressure；
The boiling point liter of sodium aluminate solution is related with the concentration in solution containing alkali and current solution temperature, in the steaming of alumina producing
It sends out in process, the boiling point under sodium aluminate solution normal pressure rises △BPERelational expression are as follows:
△BPE=c0+c1Nk+c2Tin+c3NkTin+c4Nk2+c5Tin 2+c6NkTin 2+c7Nk2Tin+c8Nk3+c9Tin 3
Wherein c0, c1, c2, c3, c4, c5, c6, c7, c8, c9For parameter, the parameter is under current production status according to discharge port
The sodium aluminate solution concentration at place obtain after production carries out polynomial regression fit to above formula with the data chemically examined, and Nk is
Caustic alkali concentration, TinFor feedstock solution temperature；
Step 3.3: △ is risen to boiling point according to Ji Xinke formulaBPEIt is modified, obtains revised boiling point and rise △ 'BPE；
Since the pressure change of solution will lead to the variation of feed liquid boiling point, according to Ji Xinke formula to the boiling under sodium aluminate solution normal pressure
Point is increased and is corrected, formula are as follows:
△′BPE=f △BPE
Wherein f is correction coefficient, its calculation formula is:
Wherein r be current production status pressure under secondary steam the latent heat of vaporization；
By carrying out regression analysis to vapor (steam) temperature and heat content table, the relational expression of steam latent heat and temperature is obtained are as follows:
Wherein d1, d2, d3It is quasi- according to return to the data in vapor (steam) temperature and heat content table under current production status for parameter
Conjunction obtains；
The boiling point that can be calculated revised sodium aluminate solution by calculating above-mentioned steps rises △ 'BPE:
Step 4: △ ' is risen according to the boiling point that step 3 obtainsBPEFlash distillation rate CFS is calculated, according to the online Real-Time Evaluation of obtained CFS
The intensity flashed in practical aluminum oxide production process, is shown below:
Wherein TinFor feedstock solution temperature, ToutFor the solution temperature that discharges, TsatFor the saturation temperature under pressure corresponding with solution,
Tsat=Tp+△′BPE；τ is residence time of the solution in flash vessel,Q is feed rate, and α is flash vessel radius, h
For liquid level in flash vessel.
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| CN201910499489.4A CN110197703B (en) | 2019-06-11 | 2019-06-11 | Flash evaporation strength evaluation method for flash evaporation process in alumina evaporation process |
| PCT/CN2019/090925 WO2020248167A2 (en) | 2019-06-11 | 2019-06-12 | Method for calculating flash evaporation speed of flash evaporation procedure in aluminum oxide evaporation process |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112729882A (en) * | 2020-11-24 | 2021-04-30 | 合肥通用机械研究院有限公司 | Performance evaluation method and test device for high-temperature heat pump type steam generator set |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101551829A (en) * | 2009-05-15 | 2009-10-07 | 中南大学 | Online predication method for concentration of export alkaline liquor of alumina evaporation device |
| CN203807189U (en) * | 2013-12-24 | 2014-09-03 | 东北大学设计研究院（有限公司） | Evaporation system used for producing aluminium oxide |
| CN104866707A (en) * | 2015-04-14 | 2015-08-26 | 中南大学 | Optimal liquid level setting method for falling-film evaporator in alumina evaporation process |
-
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- 2019-06-11 CN CN201910499489.4A patent/CN110197703B/en active Active
- 2019-06-12 WO PCT/CN2019/090925 patent/WO2020248167A2/en active Application Filing
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101551829A (en) * | 2009-05-15 | 2009-10-07 | 中南大学 | Online predication method for concentration of export alkaline liquor of alumina evaporation device |
| CN203807189U (en) * | 2013-12-24 | 2014-09-03 | 东北大学设计研究院（有限公司） | Evaporation system used for producing aluminium oxide |
| CN104866707A (en) * | 2015-04-14 | 2015-08-26 | 中南大学 | Optimal liquid level setting method for falling-film evaporator in alumina evaporation process |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112729882A (en) * | 2020-11-24 | 2021-04-30 | 合肥通用机械研究院有限公司 | Performance evaluation method and test device for high-temperature heat pump type steam generator set |
| CN112729882B (en) * | 2020-11-24 | 2022-11-29 | 合肥通用机械研究院有限公司 | Performance evaluation method and testing device for high-temperature heat pump type steam generating unit |
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| WO2020248167A2 (en) | 2020-12-17 |
| CN110197703B (en) | 2021-06-08 |
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