CN112774230A - Evaporator unit and evaporation process method - Google Patents
Evaporator unit and evaporation process method Download PDFInfo
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- CN112774230A CN112774230A CN202110030078.8A CN202110030078A CN112774230A CN 112774230 A CN112774230 A CN 112774230A CN 202110030078 A CN202110030078 A CN 202110030078A CN 112774230 A CN112774230 A CN 112774230A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/26—Multiple-effect evaporating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/06—Flash distillation
- B01D3/065—Multiple-effect flash distillation (more than two traps)
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
- C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
- C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
Abstract
The invention provides an evaporator unit and an evaporation process method, wherein the evaporator unit comprises: solution flash tank; an atmospheric condenser; the waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser, and the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the powerful unit; a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a two-effect evaporator, a one-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank which are connected in sequence; a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator; therefore, the solution flash tank concentrates the materials in advance, so that the materials are ensured to be subjected to negative pressure flash evaporation before entering the evaporator unit, the amount of evaporated water is increased, and the steam-water ratio is reduced; the steam generated by the powerful unit is used as a heat source of the first six-effect evaporator, and after the steam is secondarily utilized by the first six-effect evaporator, the temperature of the exhaust steam is reduced, the vacuum degree of the evaporation unit is improved, and the energy consumption and the production cost of the evaporation unit are reduced.
Description
Technical Field
The invention belongs to the technical field of fine alumina production, and particularly relates to an evaporator unit and an evaporation process method.
Background
At present, the Bayer process for producing and purifying alumina at home and abroad generally adopts a method that seed precipitation mother liquor is evaporated and then the evaporated mother liquor is subjected to dissolution reaction with bauxite (aluminum hydroxide). However, in practical application, along with the operation of production, more and more impurities in the solution, particularly the carbon alkali, the content of which is as high as 17 percent, are found, and the production of high-quality aluminum hydroxide is seriously influenced.
In order to reduce the content of carbon and alkali in the process, another powerful unit is started to concentrate the evaporation mother liquor in the prior art, and then the solution is purified by a filter press. However, after the powerful steam generator set is started, the steam exhaust amount is too large, so that the vacuum degree of the steam generator set is reduced by 10kpa, the optimal balance of the evaporator unit set is damaged, the energy consumption of the evaporator unit set is increased, and the production cost is seriously increased.
Disclosure of Invention
Aiming at the problems in the prior art, the embodiment of the invention provides an evaporator unit and an evaporation process method, which are used for solving the technical problem that when the evaporator unit is used for producing high-quality aluminum hydroxide in the prior art, the evaporator unit is started to reduce impurities in a solution, so that the energy consumption of the evaporator unit is increased, and further the production cost is increased.
The invention provides an evaporator unit, comprising:
the solution flash tank is used for concentrating materials;
an atmospheric condenser;
the waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser, and the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the strong-effect unit;
a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a two-effect evaporator, a one-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank which are connected in sequence;
the solution flash tank is respectively connected with the first six-effect evaporator and the second six-effect evaporator, and a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator.
Optionally, the atmospheric condenser is respectively connected with the non-condensable gas outlets of the second six-effect evaporator, the five-effect evaporator, the four-effect evaporator, the three-effect evaporator, the two-effect evaporator and the one-effect evaporator through non-condensable gas pipelines.
Optionally, the evaporator unit further includes:
and the condensate water tank is connected with the first six-effect evaporator and is used for recovering condensate water of the first six-effect evaporator.
Optionally, a waste steam outlet of the solution flash tank is connected to the atmospheric condenser and a waste steam inlet of the first six-effect evaporator respectively.
Optionally, the evaporator set further includes:
and the steam-water separator is connected with the outlet of the atmospheric condenser and is used for drying the non-condensable gas output by the atmospheric condenser.
Optionally, the evaporator set further includes:
the first material passing pump is arranged between the solution flash tank and the first six-effect evaporator;
the second material passing pump is arranged between the solution flash tank and the second six-effect evaporator;
the third material passing pump is arranged between the first six-effect evaporator and the fifth-effect evaporator;
the fourth material passing pump is arranged between the second six-effect evaporator and the fifth-effect evaporator;
the fifth material passing pump is arranged between the five-effect evaporator and the four-effect evaporator;
the sixth material passing pump is arranged between the four-effect evaporator and the three-effect evaporator;
the seventh material passing pump is arranged between the three-effect evaporator and the two-effect evaporator;
and the eighth material passing pump is arranged between the second-effect evaporator and the first-effect evaporator.
Optionally, the evaporator set further includes:
the first circulating pump is arranged between the material outlet and the material inlet of the first six-effect evaporator;
the second circulating pump is arranged between the material outlet and the material inlet of the second six-effect evaporator;
the third circulating pump is arranged between the material outlet and the material inlet of the five-effect evaporator;
the fourth circulating pump is arranged between the material outlet and the material inlet of the four-effect evaporator;
the fifth circulating pump is arranged between the material outlet and the material inlet of the three-effect evaporator;
the sixth circulating pump is arranged between the material outlet and the material inlet of the second-effect evaporator;
and the seventh circulating pump is arranged between the material outlet and the material inlet of the first-effect evaporator.
Optionally, the evaporator unit further includes:
the first preheater is arranged between the second six-effect evaporator and the five-effect evaporator;
the second preheater is arranged between the five-effect evaporator and the four-effect evaporator;
the third preheater is arranged between the four-effect evaporator and the three-effect evaporator;
the fourth preheater is arranged between the three-effect evaporator and the two-effect evaporator;
and the fifth preheater is arranged between the second-effect evaporator and the first-effect evaporator.
Optionally, the material concentrations output by the first six-effect evaporator and the second six-effect evaporator are the same.
The invention also provides an evaporation process method which is applied to the evaporator unit, and the method comprises the following steps:
concentrating the material by using the solution flash tank;
according to a preset material distribution strategy, conveying the concentrated materials to the first six-effect evaporator and the second six-effect evaporator respectively;
and evaporating the concentrated material by a countercurrent evaporation mode to obtain a solution product.
The invention provides an evaporator unit and an evaporation process method, wherein the evaporator unit comprises: the solution flash tank is used for concentrating materials; an atmospheric condenser; the waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser, and the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the strong-effect unit; a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a two-effect evaporator, a one-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank which are connected in sequence; the solution flash tank is respectively connected with the first six-effect evaporator and the second six-effect evaporator, and a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator; therefore, the material is concentrated in advance by the solution flash tank and then enters the evaporation unit, so that the material is ensured to be subjected to negative pressure flash evaporation before entering the evaporator unit, the evaporation water quantity is increased, and the steam-water ratio is reduced; meanwhile, the phenomenon that the temperature of exhaust steam generated by the second six-effect evaporator is increased due to overhigh material temperature, so that the vacuum degree of an evaporation unit is reduced can be avoided; and even if the strong-effect unit generates exhaust steam with higher temperature, the exhaust steam is used as a heat source of the first six-effect evaporator, and the temperature of the exhaust steam is reduced after the exhaust steam is secondarily utilized by the first six-effect evaporator, so that the temperature in the atmospheric condenser can not be increased after the exhaust steam generated by the first six-effect evaporator enters the atmospheric condenser, the vacuum degree of the evaporation unit can be further improved, the steam-water ratio of the evaporation unit is reduced, the evaporation water quantity is increased, and the production cost is further reduced.
Drawings
Fig. 1 is a schematic overall structure diagram of an evaporator unit according to an embodiment of the present invention;
FIG. 2 is a schematic flow diagram of an evaporation process provided by an embodiment of the present invention;
FIG. 3 is a diagram illustrating a statistical result of the water evaporation amount of the evaporator unit according to the present invention;
fig. 4 is a schematic diagram of a statistical result of steam-water ratios of an evaporator unit in the prior art and an evaporator unit provided by the present invention.
Detailed Description
In order to solve the technical problem that when an evaporator unit is used for producing high-quality aluminum hydride in the prior art, the energy consumption of the evaporator unit is increased due to the fact that a powerful unit is started to reduce impurities in solution, and then the production cost is increased. The invention provides an evaporator unit and an evaporation process method.
The technical solution of the present invention is further described in detail by the accompanying drawings and the specific embodiments.
Example one
This embodiment provides an evaporator unit, as shown in fig. 1, the evaporator unit includes: the system comprises a solution flash tank 1, a first-effect evaporator 2, a second-effect evaporator 3, a third-effect evaporator 4, a fourth-effect evaporator 5, a fifth-effect evaporator 6, a first sixth-effect evaporator 7, a second sixth-effect evaporator 8, a first flash tank 9, a second flash tank 10, a third flash tank 11, a fourth flash tank and an atmospheric condenser 12, wherein the first flash tank is connected with the solution flash tank 1; wherein the content of the first and second substances,
the solution flash tank 1 is respectively connected with material inlets of a first six-effect evaporator 7 and a second six-effect evaporator 8 through material pipelines A1; the solution flash tank 1 is used for concentrating the material to reduce the temperature of the material;
the exhaust steam outlet of the first six-effect evaporator 7 is connected with the atmospheric condenser 13 through an exhaust steam pipeline B3, the exhaust steam inlet of the first six-effect evaporator 7 is connected with the exhaust steam outlet of the strong effect unit 14 through an exhaust steam pipeline B2, and the exhaust steam generated by the strong effect unit 14 is used as the heat source of the first six-effect evaporator 7. Here, the exhaust steam generated by the powerful unit 14 directly enters the first six-effect evaporator 7, even if the powerful unit 14 generates exhaust steam with higher temperature, the exhaust steam is used as a heat source of the first six-effect evaporator 7, and after the exhaust steam is secondarily used by the first six-effect evaporator 7, the temperature of the exhaust steam is reduced, so that the temperature in the atmospheric condenser 13 cannot be increased after the exhaust steam generated by the first six-effect evaporator 7 enters the atmospheric condenser 13, and because the atmospheric condenser 13 is used for providing a vacuum environment for the whole evaporation unit, the vacuum degree of the evaporation unit can be increased, the operation efficiency of the evaporation unit is further improved, and the energy consumption is reduced.
The second six-effect evaporator 8, the fifth-effect evaporator 6, the fourth-effect evaporator 5, the third-effect evaporator 4, the second-effect evaporator 3, the first-effect evaporator 2, the first flash tank 9, the second flash tank 10, the third flash tank 11 and the fourth flash tank 12 are sequentially connected through material pipelines. That is, the material outlet of the second six-effect evaporator 8 is connected with the material inlet of the fifth-effect evaporator 6 through a corresponding material pipeline, the material outlet of the fifth-effect evaporator 6 is connected with the material inlet of the fourth-effect evaporator 5 through a corresponding material pipeline, the material outlet of the fourth-effect evaporator 5 is connected with the material inlet of the third-effect evaporator 4 through a corresponding material pipeline, the material outlet of the third-effect evaporator 4 is connected with the material inlet of the second-effect evaporator 3 through a corresponding material pipeline, the material outlet of the second-effect evaporator 3 is connected with the material inlet of the first-effect evaporator 2 through a corresponding material pipeline, the material outlet of the first-effect evaporator 2 is connected with the material inlet of the first flash tank 9 through a corresponding material pipeline, the material outlet of the first flash tank 9 is connected with the material inlet of the second flash tank 10 through a corresponding material pipeline, the material outlet of the second flash tank 10 is connected with the material inlet of the third flash tank 11 through a corresponding material pipeline, the material outlet of the third flash tank 11 is connected with the material inlet of the fourth flash tank 12 through a corresponding material pipeline. In addition, a material inlet of the five-effect evaporator 6 is connected with a material outlet of the first six-effect evaporator 7.
The atmospheric condenser 13 is respectively connected with the second six-effect evaporator 8, the five-effect evaporator 6, the four-effect evaporator 5, the three-effect evaporator 4, the two-effect evaporator 3 and the one-effect evaporator 2 through a non-condensable gas pipeline B, and the atmospheric condenser 13 is used for pumping out non-condensable gas for the second six-effect evaporator 8, the five-effect evaporator 6, the four-effect evaporator 5, the three-effect evaporator 4, the two-effect evaporator 3 and the one-effect evaporator 2.
As an alternative embodiment, the dead steam generated by the solution flash tank 1 may comprise three passes. A first path: the exhaust steam outlet of the solution flash tank 1 is connected with the atmospheric condenser 13 through an exhaust steam channel B1, so that the exhaust steam generated by the solution flash tank 1 enters the atmospheric condenser 13 through an exhaust steam channel B1; a second path: the dead steam generated by the solution flash tank 1 is connected with a dead steam channel of the five-effect evaporator 6 through a dead steam channel B4, and the dead steam enters the second six-effect evaporator 8; a third path: the dead steam generated by the solution flash tank 1 is connected with a dead steam inlet of the first six-effect evaporator 7 through a dead steam channel B5 and is used as a heat source of the first six-effect evaporator 7. It is worth noting that the first passage, the second passage and the third passage are all provided with control valves, the first passage and the third passage are not opened at the same time, and are selected for use according to the material temperature; the second passage is a standby passage, and when the temperature of the steam unit does not reach the preset target temperature, the second passage can be controlled to be opened.
For example, if the material temperature is less than 82 ℃, the first passage may be controlled to be opened, and the solution flash tank 1 is used to concentrate the material in advance, so as to reduce the material temperature. Specifically, the exhaust steam of the solution flash tank 1 is directly connected with the atmospheric condenser 13 to reduce the boiling point of the material, and then negative pressure flash evaporation is carried out on the material in the solution flash tank 1, so that the material can be concentrated in advance, and the temperature of the material is reduced. Wherein when the initial concentration of the material is 155g/L, the concentration of the concentrated material can be 158-162 g/L.
If the temperature of the material still does not reach the preset target temperature after the material is concentrated, the first passage can be controlled to be closed, the second passage is controlled to be opened, the exhaust steam generated by the solution flash tank 1 can be used as a heat source of the second six-effect evaporator 8, the exhaust steam generated by the second six-effect evaporator 8 can be reduced in temperature after the exhaust steam is secondarily utilized by the second six-effect evaporator 8, and the temperature of the evaporation unit is further reduced.
If the temperature of the material is higher than 82 ℃, the third passage can be controlled to be opened at the moment. The material is concentrated by using negative pressure flash evaporation, after the temperature of the material is reduced, the exhaust steam generated by the solution flash tank 1 directly enters the first six-effect evaporator 7, and the evaporation speed of the first six-effect evaporator 7 can be increased due to the fact that the temperature of the exhaust steam is higher.
Here, negative pressure is applied to the four-effect evaporator 5, the five-effect evaporator 6, the first six-effect evaporator 7 and the second six-effect evaporator 8; the pressure in the first-effect evaporator 2 and the second-effect evaporator 3 is positive pressure, and the pressure of the third-effect evaporator 4 is 0.
After the material is concentrated, the concentrated material is conveyed to a first six-effect evaporator 7 and a second six-effect evaporator 8 based on a preset distribution proportion. Generally, the concentration of the materials conveyed by the first six-effect evaporator 7 and the second six-effect evaporator 8 should be kept consistent, in order to ensure that the concentration of the materials conveyed by the first six-effect evaporator 7 and the second six-effect evaporator 8 is kept consistent, the proportion of the materials in the first six-effect evaporator 7 is about 30-40%, and the rest of the materials are conveyed to the second six-effect evaporator 8.
With continued reference to fig. 1, the evaporator unit further comprises: and the condensed water tank 15 is connected with the first six-effect evaporator 7, and is used for recovering the condensed water of the first six-effect evaporator 7. Wherein the condensed water tank 15 is also connected with the first six-effect evaporator 7 through a dead steam pipeline B6.
Here, the present embodiment adopts a countercurrent contact evaporation process to evaporate the material, that is, the flow direction of the material is: the system comprises a solution flash tank 1, a first six-effect evaporator 7, a second six-effect evaporator 8, a five-effect evaporator 6, a four-effect evaporator 5, a three-effect evaporator 4, a two-effect evaporator 3, a one-effect evaporator 2, a first flash tank 9, a second flash tank 10, a third flash tank 11 and a fourth flash tank 12, and product solution is output from the fourth flash tank 12.
Then, the flow direction of the dead steam generated by each effect evaporator is as follows: a first-effect evaporator 2, a second-effect evaporator 3, a third-effect evaporator 4, a fourth-effect evaporator 5, a fifth-effect evaporator 6, a second sixth-effect evaporator 8 and an atmospheric condenser 13. Wherein an exhaust steam channel B7 is arranged between the first-effect evaporator 2 and the second-effect evaporator 3, an exhaust steam channel B8 is arranged between the second-effect evaporator 3 and the third-effect evaporator 4, an exhaust steam channel B9 is arranged between the third-effect evaporator 4 and the fourth-effect evaporator 5, an exhaust steam channel B10 is arranged between the fourth-effect evaporator 5 and the fifth-effect evaporator 6, an exhaust steam channel B11 is arranged between the fifth-effect evaporator 6 and the second sixth-effect evaporator 8, and an exhaust steam channel B12 is arranged between the second sixth-effect evaporator 8 and the atmospheric condenser 13.
Furthermore, in order to save the gas consumption of the evaporation unit, the dead steam generated by each flash tank can be recycled. Specifically, the exhaust steam generated by the first flash tank 9 enters the second-effect evaporator 3 through an exhaust steam pipeline B13, the exhaust steam generated by the second flash tank 10 enters the third-effect evaporator 4 through an exhaust steam pipeline B14, the exhaust steam generated by the third flash tank 11 enters the fourth-effect evaporator 5 through an exhaust steam pipeline B15, and the exhaust steam generated by the fourth flash tank 12 enters the fifth-effect evaporator 6 through an exhaust steam pipeline B16.
In order to dry the steam output by the atmospheric condenser, with continued reference to fig. 1, the evaporation plant further comprises: a steam-water separator 16; the steam-water separator 16 is connected with the outlet of the atmospheric condenser 13, and the steam-water separator 16 is used for drying the non-condensable gas output by the atmospheric condenser 13.
Further, in order to enable the material to be transported between the individual effect evaporators, with continued reference to fig. 1, the evaporation plant further comprises: a first material passing pump C1, a second material passing pump C2, a third material passing pump C3, a fourth material passing pump C4, a fifth material passing pump C5, a sixth material passing pump C6, a seventh material passing pump C7 and an eighth material passing pump C8; wherein the content of the first and second substances,
the first material passing pump C1 is arranged between the solution flash tank 1 and the first six-effect evaporator 7, the second material passing pump C2 is arranged between the solution flash tank 1 and the second six-effect evaporator 8, the third material passing pump C3 is arranged between the first six-effect evaporator 7 and the fifth-effect evaporator 6, the fourth material passing pump C4 is arranged between the second six-effect evaporator 8 and the fifth-effect evaporator 6, the fifth material passing pump C5 is arranged between the fifth-effect evaporator 6 and the fourth-effect evaporator 5, the sixth material passing pump C6 is arranged between the fourth-effect evaporator 5 and the third-effect evaporator 4, the seventh material passing pump C7 is arranged between the third-effect evaporator 4 and the second-effect evaporator 3, and the eighth material passing pump C8 is arranged between the second-effect evaporator 3 and the first-effect evaporator 2.
In order to improve the cyclic utilization of material, reduction in production cost, the evaporation unit still includes: first circulating pump D1, second circulating pump D2, third circulating pump D3, fourth circulating pump D4, fifth circulating pump D6, sixth circulating pump D6, and seventh circulating pump D7; wherein the content of the first and second substances,
first circulating pump D1 sets up between the material export of first six-effect evaporator 7 and material inlet, second circulating pump D2 sets up between the material export of second six-effect evaporator 8 and material inlet, third circulating pump D3 sets up between the material export of five-effect evaporator 6 and material inlet, fourth circulating pump D4 sets up between the material export of four-effect evaporator 5 and material inlet, fifth circulating pump D6 sets up between the material export of three-effect evaporator 4 and material inlet, sixth circulating pump D6 sets up between the material export of two-effect evaporator 3 and material inlet, seventh circulating pump D7 sets up between the material export of one-effect evaporator 2 and material inlet.
Here, because the material temperature of each effect evaporator output all has preset requirement, therefore the evaporation unit still includes: a first preheater E1, a second preheater E2, a third preheater E3, a fourth preheater E4, and a fifth preheater E5; wherein the content of the first and second substances,
the first preheater E1 is arranged between the second six-effect evaporator 8 and the five-effect evaporator 6, the second preheater E2 is arranged between the five-effect evaporator 6 and the four-effect evaporator 5, the third preheater E3 is arranged between the four-effect evaporator 5 and the three-effect evaporator 4, the fourth preheater E4 is arranged between the three-effect evaporator 4 and the two-effect evaporator 3, and the fifth preheater E5 is arranged between the two-effect evaporator 3 and the one-effect evaporator 2.
It is to be noted that the exhaust steam generated by the first flash tank 9 needs to be preheated by the fourth preheater E4 and then enters the second-effect evaporator 3, the exhaust steam generated by the second flash tank 10 needs to be preheated by the third preheater E3 and then enters the third-effect evaporator 4, the exhaust steam generated by the third flash tank 11 needs to be preheated by the second preheater E2 and then enters the fourth-effect evaporator 5, and the exhaust steam generated by the fourth flash tank 12 needs to be preheated by the first preheater E1 and then enters the fifth-effect evaporator 6.
Thus, in the embodiment, the exhaust steam generated by the powerful unit 14 is used as the heat source of the first six-effect evaporator 7, even if the powerful unit 14 generates exhaust steam with higher temperature, the exhaust steam is used as the heat source of the first six-effect evaporator 7, and after the exhaust steam is secondarily utilized by the first six-effect evaporator 7, the temperature of the exhaust steam is reduced, so that the temperature in the atmospheric condenser 13 is not increased after the exhaust steam generated by the first six-effect evaporator 7 enters the atmospheric condenser 13, and the vacuum degree of the evaporating unit can be further increased; the solution flash tank 1 can be used for concentrating the material in advance and then feeding the concentrated material into the evaporation unit, so that the material is ensured to be subjected to negative pressure flash evaporation before entering the evaporator unit, the evaporation water quantity is increased, and the steam-water ratio is reduced; meanwhile, the phenomenon that the temperature of exhaust steam generated by the second six-effect evaporator 8 is increased due to overhigh material temperature and the vacuum degree of the evaporation unit is reduced can be avoided, the vacuum degree of the evaporation unit is further ensured, the operation efficiency of the evaporation unit is ensured, the steam-water ratio of the evaporation unit is reduced, the steam water quantity is improved, and the production cost is reduced.
Based on the same inventive concept, the invention also provides an evaporation process method, which is detailed in example II.
Example two
The present embodiment provides an evaporation process method, which is applied to the evaporator unit provided in the first embodiment, wherein the evaporator unit includes: the system comprises a solution flash tank, a first-effect evaporator, a second-effect evaporator, a third-effect evaporator, a fourth-effect evaporator, a fifth-effect evaporator, a first sixth-effect evaporator, a second sixth-effect evaporator, a first flash tank, a second flash tank, a third flash tank, a fourth flash tank and an atmospheric condenser. As shown in fig. 2, the method includes:
s210, concentrating the material by using a solution flash tank;
here, the solution flash tank is respectively connected with the material inlets of the first six-effect evaporator and the second six-effect evaporator through material pipelines; the solution flash tank is used for concentrating the material to reduce the temperature of the material.
The waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser through a waste steam pipeline, the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the powerful unit through a waste steam pipeline, and the waste steam generated by the powerful unit is used as a heat source of the first six-effect evaporator. Here, because the exhaust steam that the powerful unit produced has directly got into first six effect evaporimeters, even the powerful unit has produced the exhaust steam of higher temperature, this exhaust steam is as the heat source of first six effect evaporimeters, after first six effect evaporimeters reutilization, the exhaust steam temperature reduces, so the exhaust steam that first six effect evaporimeters produced again gets into the atmosphere condenser after, can not lead to the temperature rise in the atmosphere condenser, because of the atmosphere condenser is used for providing the vacuum environment for whole evaporimeter unit, consequently can improve the vacuum degree of evaporimeter unit, and then improve the operating efficiency of evaporimeter unit, reduce the energy consumption.
The second six-effect evaporator, the fifth-effect evaporator, the fourth-effect evaporator, the third-effect evaporator, the second-effect evaporator, the first flash tank, the second flash tank, the third flash tank and the fourth flash tank are sequentially connected through material pipelines. That is, the material outlet of the second six-effect evaporator is connected with the material inlet of the fifth-effect evaporator through a corresponding material pipeline, the material outlet of the fifth-effect evaporator is connected with the material inlet of the fourth-effect evaporator through a corresponding material pipeline, the material outlet of the fourth-effect evaporator is connected with the material inlet of the third-effect evaporator through a corresponding material pipeline, the material outlet of the third-effect evaporator is connected with the material inlet of the second-effect evaporator through a corresponding material pipeline, the material outlet of the second-effect evaporator is connected with the material inlet of the first flash tank through a corresponding material pipeline, the material outlet of the first flash tank is connected with the material inlet of the second flash tank through a corresponding material pipeline, the material outlet of the second flash tank is connected with the material inlet of the third flash tank through a corresponding material pipeline, and the material outlet of the third flash tank is connected with the material inlet of the fourth flash tank through a corresponding material pipeline. In addition, a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator. In addition, a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator.
The atmospheric condenser is respectively connected with the second six-effect evaporator, the five-effect evaporator, the four-effect evaporator, the three-effect evaporator, the two-effect evaporator and the one-effect evaporator through non-condensable gas pipelines, and is used for pumping out non-condensable gas from the second six-effect evaporator, the five-effect evaporator, the four-effect evaporator, the three-effect evaporator, the two-effect evaporator and the one-effect evaporator.
As an alternative embodiment, the dead steam produced by the solution flash tank may comprise three passes. A first path: a dead steam outlet of the solution flash tank is connected with an atmospheric condenser through a dead steam channel, so that dead steam generated by the solution flash tank enters the atmospheric condenser; a second path: the dead steam generated by the solution flash tank is connected with a dead steam channel of the five-effect evaporator through a dead steam channel, and the dead steam enters the second six-effect evaporator; a third path: and dead steam generated by the solution flash tank is connected with a dead steam inlet of the first six-effect evaporator through a dead steam channel and is used as a heat source of the first six-effect evaporator. It is worth noting that the first passage, the second passage and the third passage are all provided with control valves, the first passage and the third passage are not opened at the same time, and are selected for use according to the material temperature; the second passage is a standby passage and can be controlled to be opened when the temperature of the steam unit does not reach the preset target temperature.
For example, if the temperature of the material is less than 82 ℃, the first passage may be controlled to be opened, and the solution flash tank is used to concentrate the material to reduce the temperature of the material. Specifically, the exhaust steam of the solution flash tank is directly connected with the atmospheric condenser, so that the boiling point of the material can be reduced, and the material is subjected to negative pressure flash evaporation in the solution flash tank, so that the material is concentrated, and the temperature of the material is reduced. When the initial concentration of the material is 155g/L, the concentration of the concentrated material can be 158-162 g/L.
If the temperature of the material still does not reach the preset target temperature after the material is concentrated, the first passage is closed at the moment, the second passage is controlled to be opened, the exhaust steam generated by the solution flash tank can be used as a heat source of the second six-effect evaporator, the temperature of the exhaust steam generated by the second six-effect evaporator can be reduced after the exhaust steam is secondarily utilized by the second six-effect evaporator, and the temperature of an evaporation unit is further reduced.
If the temperature of the material is higher than 82 ℃, the third passage can be controlled to be opened. The material is concentrated by using negative pressure flash evaporation, after the temperature of the material is reduced, the exhaust steam generated by the solution flash tank directly enters the first six-effect evaporator, and the evaporation speed of the first six-effect evaporator can be increased due to the fact that the temperature of the exhaust steam is higher.
Here, negative pressure is applied to the four-effect evaporator, the five-effect evaporator, the first six-effect evaporator and the second six-effect evaporator; the pressure in the first-effect evaporator and the second-effect evaporator is positive pressure, and the pressure of the third-effect evaporator is 0.
S211, conveying the concentrated materials to a first six-effect evaporator and a second six-effect evaporator respectively according to a preset material distribution strategy;
after the materials are concentrated, the concentrated materials are conveyed to a first six-effect evaporator and a second six-effect evaporator based on a preset material distribution strategy, generally speaking, the concentrations of the materials conveyed by the first six-effect evaporator and the second six-effect evaporator are kept consistent, in order to ensure that the concentrations of the materials conveyed by the first six-effect evaporator and the second six-effect evaporator are kept consistent, the proportion of the materials in the first six-effect evaporator is about 30-40%, and the rest of the materials are conveyed to the second six-effect evaporator.
S212, evaporating the concentrated material by using a countercurrent evaporation mode to obtain a solution product.
And then evaporating the concentrated material by a countercurrent evaporation mode to obtain a solution product.
Here, the present embodiment adopts a countercurrent contact evaporation process to evaporate the material, that is, the flow direction of the material is: the system comprises a solution flash tank, a first six-effect evaporator, a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a second-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank, wherein a product solution is output from the fourth flash tank.
Then, the flow direction of the dead steam generated by each effect evaporator is as follows: a first-effect evaporator, a second-effect evaporator, a third-effect evaporator, a fourth-effect evaporator, a fifth-effect evaporator, a second sixth-effect evaporator and an atmospheric condenser. The system comprises a first effect evaporator, a second effect evaporator, a third effect evaporator, a fourth effect evaporator, a fifth effect evaporator and an atmospheric condenser, wherein a corresponding steam exhaust channel is arranged between the first effect evaporator and the second effect evaporator, a steam exhaust channel is arranged between the second effect evaporator and the third effect evaporator, a corresponding steam exhaust channel is arranged between the third effect evaporator and the fourth effect evaporator, a corresponding steam exhaust channel is arranged between the fourth effect evaporator and the fifth effect evaporator, a corresponding steam exhaust channel is arranged between the fifth effect evaporator and the second sixth effect evaporator, and a corresponding steam exhaust channel is arranged between the second sixth effect evaporator and.
In order to dry the steam output by the atmospheric condenser, the evaporation unit further comprises: a steam-water separator; the steam-water separator is connected with an outlet of the atmospheric condenser and is used for drying the non-condensable gas output by the atmospheric condenser.
Further, in order to enable the material to be transported between the individual effect evaporators, with continued reference to fig. 1, the evaporation plant further comprises: the first material passing pump, the second material passing pump, the third material passing pump, the fourth material passing pump, the fifth material passing pump, the sixth material passing pump, the seventh material passing pump and the eighth material passing pump; wherein the content of the first and second substances,
the first material passing pump is arranged between the solution flash tank and the first six-effect evaporator, the second material passing pump is arranged between the solution flash tank and the second six-effect evaporator, the third material passing pump is arranged between the first six-effect evaporator and the fifth-effect evaporator, the fourth material passing pump is arranged between the second six-effect evaporator and the fifth-effect evaporator, the fifth material passing pump is arranged between the fifth-effect evaporator and the fourth-effect evaporator, the sixth material passing pump is arranged between the fourth-effect evaporator and the third-effect evaporator, the seventh material passing pump is arranged between the third-effect evaporator and the second-effect evaporator, and the eighth material passing pump is arranged between the second-effect evaporator and the first-effect evaporator.
In order to improve the cyclic utilization of material, reduction in production cost, the evaporation unit still includes: the first circulating pump, the second circulating pump, the third circulating pump, the fourth circulating pump, the fifth circulating pump, the sixth circulating pump and the seventh circulating pump; wherein the content of the first and second substances,
the first circulating pump sets up between the material export and the material inlet of first six effect evaporimeter, the second circulating pump sets up between the material export and the material inlet of second six effect evaporimeter, the third circulating pump sets up between the material export and the material inlet of five effect evaporimeters, the fourth circulating pump sets up between the material export and the material inlet of four effect evaporimeters, the fifth circulating pump sets up between the material export and the material inlet of three effect evaporimeters, the sixth circulating pump sets up between the material export and the material inlet of two effect evaporimeters, the seventh circulating pump sets up between the material export and the material inlet of one effect evaporimeter.
Here, because the material temperature of each effect evaporator output all has preset requirement, therefore the evaporation unit still includes: the system comprises a first preheater, a second preheater, a third preheater, a fourth preheater and a fifth preheater; wherein the content of the first and second substances,
the first preheater is arranged between the second six-effect evaporator and the five-effect evaporator, the second preheater is arranged between the five-effect evaporator and the four-effect evaporator, the third preheater is arranged between the four-effect evaporator and the three-effect evaporator, the fourth preheater is arranged between the three-effect evaporator and the two-effect evaporator, and the fifth preheater is arranged between the two-effect evaporator and the one-effect evaporator.
The dead steam generated by the first flash tank is preheated by the fourth preheater and then enters the second-effect evaporator, the dead steam generated by the second flash tank is preheated by the third preheater and then enters the third-effect evaporator, the dead steam generated by the third flash tank is preheated by the second preheater and then enters the fourth-effect evaporator, and the dead steam generated by the fourth flash tank is preheated by the first preheater and then enters the fifth-effect evaporator.
Therefore, in the embodiment, the exhaust steam generated by the powerful unit is used as the heat source of the first six-effect evaporator, even if the powerful unit generates exhaust steam with higher temperature, the exhaust steam is used as the heat source of the first six-effect evaporator, and after the exhaust steam is secondarily utilized by the first six-effect evaporator, the temperature of the exhaust steam is reduced, so that the temperature in the atmospheric condenser cannot be increased after the exhaust steam generated by the first six-effect evaporator enters the atmospheric condenser, and the vacuum degree of the evaporating unit can be further improved; and the solution flash tank can be used for concentrating the material in advance and then entering the evaporation unit, so that the problem that the vacuum degree of the evaporation unit is reduced due to the fact that the temperature of the exhaust steam generated by the second six-effect evaporator is increased due to overhigh temperature of the material can be avoided, the vacuum degree of the evaporation unit is further ensured, the operation efficiency of the unit is improved, and the energy consumption of the unit is reduced.
The evaporator unit and the evaporation process method provided by the embodiment of the invention have the beneficial effects that at least:
the invention provides an evaporator unit and an evaporation process method, wherein the evaporator unit comprises: the solution flash tank is used for concentrating materials; an atmospheric condenser; the waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser, and the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the strong-effect unit; a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a two-effect evaporator, a one-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank which are connected in sequence; the solution flash tank is respectively connected with the first six-effect evaporator and the second six-effect evaporator, and a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator; therefore, the material is concentrated in advance by the solution flash tank and then enters the evaporation unit, so that the material is ensured to be subjected to negative pressure flash evaporation before entering the evaporator unit, the evaporation water quantity is increased, and the steam-water ratio is reduced; meanwhile, the phenomenon that the temperature of exhaust steam generated by the second six-effect evaporator is increased due to overhigh material temperature, so that the vacuum degree of an evaporation unit is reduced can be avoided; and even if the strong-effect unit generates exhaust steam with higher temperature, the exhaust steam is used as a heat source of the first six-effect evaporator, and after the exhaust steam is secondarily utilized by the first six-effect evaporator, the temperature of the exhaust steam is reduced, so that the exhaust steam generated by the first six-effect evaporator cannot cause the temperature in the atmospheric condenser to rise after entering the atmospheric condenser, the vacuum degree of the evaporation unit can be further improved, the operation efficiency of the evaporation unit is ensured, the steam-water ratio of the evaporation unit is reduced, the evaporation water quantity is improved, and further the production cost is reduced.
EXAMPLE III
In practical application, when a material is evaporated by using the evaporator unit provided in the first embodiment and the evaporation process method provided in the second embodiment, the operation control indexes of the evaporator unit are shown in table 1:
TABLE 1
| Item | Index (I) |
| Solution flash tank feed (m)3/h) | 600-700 |
| Second six effect evaporator feed rate (m)3/h) | 300- |
| First six effect evaporator feed rate (m)3/h) | 200- |
| Stock solution NK g/L | 150-160 |
| The temperature of the stock solution of the material is lower | 70-80 |
| Vacuum degree kpa | -70～-90 |
| Pressure kpa of one-effect evaporator | 350-450 |
| Second six-effect evaporator steam chamber pressure kpa | -40～-50 |
| First six-effect evaporator effective steam chamber pressure kpa | -10～-20 |
| Pressure kpa of solution flash tank | -60～-80 |
| Fourth flash tank discharging NK g/L | 190-200 |
| Effective evaporation water amount t/h of first six-effect evaporator | 13-18 |
| The amount of liquid evaporation water in the solution flash evaporation tank is t/h | 5-10 |
| First six-effect evaporator NK g/L | 170-175 |
| Solution flash tank NK g/L | 160-170 |
In table 1, NK is the concentration of NaOH in the solution, and compared with the evaporator set in the prior art, the solution flash tank is used for flash evaporation and concentration before the material enters the evaporator set, so that the evaporation amount of the evaporator set is averagely increased by 12.5%, and the steam-water ratio is reduced by 13%; for the powerful units, the steam-water ratio of the powerful units is reduced by 16%, and the gas consumption is reduced by 20%.
Wherein, the statistical results of the evaporation water amount of the evaporator unit in the prior art and the evaporator unit provided by the invention are shown in fig. 3; the statistical result of the steam-water ratio of the evaporator unit in the prior art and the evaporator unit provided by the invention is shown in fig. 4. As can be seen from fig. 3, the amount of water evaporated (reference F) by the evaporator unit of the present invention is significantly higher than the amount of water evaporated (reference E) by the evaporator unit of the prior art; as can be seen from fig. 4, the steam-water ratio (mark K) of the evaporator unit of the present invention is significantly lower than that (mark G) of the evaporator unit in the prior art; the evaporator unit provided by the invention can reduce energy consumption and improve operation efficiency.
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, and any modifications, equivalents, improvements, etc. that are within the spirit and principle of the present invention should be included in the present invention.
Claims (10)
1. An evaporator unit, comprising:
the solution flash tank is used for concentrating materials;
an atmospheric condenser;
the waste steam outlet of the first six-effect evaporator is connected with the atmospheric condenser, and the waste steam inlet of the first six-effect evaporator is connected with the waste steam outlet of the strong-effect unit;
a second six-effect evaporator, a five-effect evaporator, a four-effect evaporator, a three-effect evaporator, a two-effect evaporator, a one-effect evaporator, a first flash tank, a second flash tank, a third flash tank and a fourth flash tank which are connected in sequence;
the solution flash tank is respectively connected with the first six-effect evaporator and the second six-effect evaporator, and a material inlet of the five-effect evaporator is connected with a material outlet of the first six-effect evaporator.
2. The evaporator unit according to claim 1, wherein the atmospheric condenser is connected to non-condensable gas outlets of the second six-effect evaporator, the five-effect evaporator, the four-effect evaporator, the three-effect evaporator, the two-effect evaporator and the one-effect evaporator through non-condensable gas pipes, respectively.
3. The evaporator unit of claim 1, further comprising:
and the condensate water tank is connected with the first six-effect evaporator and is used for recovering condensate water of the first six-effect evaporator.
4. The evaporator unit of claim 1, wherein the dead-steam outlet of the solution flash tank is connected to the atmospheric condenser and the dead-steam inlet of the first six-effect evaporator, respectively.
5. The evaporator unit of claim 1, further comprising:
and the steam-water separator is connected with the outlet of the atmospheric condenser and is used for drying the non-condensable gas output by the atmospheric condenser.
6. The evaporator unit of claim 1, further comprising:
the first material passing pump is arranged between the solution flash tank and the first six-effect evaporator;
the second material passing pump is arranged between the solution flash tank and the second six-effect evaporator;
the third material passing pump is arranged between the first six-effect evaporator and the fifth-effect evaporator;
the fourth material passing pump is arranged between the second six-effect evaporator and the fifth-effect evaporator;
the fifth material passing pump is arranged between the five-effect evaporator and the four-effect evaporator;
the sixth material passing pump is arranged between the four-effect evaporator and the three-effect evaporator;
the seventh material passing pump is arranged between the three-effect evaporator and the two-effect evaporator;
and the eighth material passing pump is arranged between the second-effect evaporator and the first-effect evaporator.
7. The evaporator unit of claim 1, further comprising:
the first circulating pump is arranged between the material outlet and the material inlet of the first six-effect evaporator;
the second circulating pump is arranged between the material outlet and the material inlet of the second six-effect evaporator;
the third circulating pump is arranged between the material outlet and the material inlet of the five-effect evaporator;
the fourth circulating pump is arranged between the material outlet and the material inlet of the four-effect evaporator;
the fifth circulating pump is arranged between the material outlet and the material inlet of the three-effect evaporator;
the sixth circulating pump is arranged between the material outlet and the material inlet of the second-effect evaporator;
and the seventh circulating pump is arranged between the material outlet and the material inlet of the first-effect evaporator.
8. The evaporator unit of claim 1, further comprising:
the first preheater is arranged between the second six-effect evaporator and the five-effect evaporator;
the second preheater is arranged between the five-effect evaporator and the four-effect evaporator;
the third preheater is arranged between the four-effect evaporator and the three-effect evaporator;
the fourth preheater is arranged between the three-effect evaporator and the two-effect evaporator;
and the fifth preheater is arranged between the second-effect evaporator and the first-effect evaporator.
9. The evaporator unit of claim 1, wherein the first six-effect evaporator and the second six-effect evaporator output a material concentration that is consistent.
10. An evaporation process method, applied to an evaporator unit according to any one of claims 1 to 9, comprising:
concentrating the material by using a solution flash tank;
according to a preset material distribution strategy, conveying the concentrated materials to a first six-effect evaporator and a second six-effect evaporator respectively;
and evaporating the concentrated material by a countercurrent evaporation mode to obtain a solution product.
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