CN102225779A - High-pressure dissolution system and method for bauxite - Google Patents
High-pressure dissolution system and method for bauxite Download PDFInfo
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- CN102225779A CN102225779A CN2011101211504A CN201110121150A CN102225779A CN 102225779 A CN102225779 A CN 102225779A CN 2011101211504 A CN2011101211504 A CN 2011101211504A CN 201110121150 A CN201110121150 A CN 201110121150A CN 102225779 A CN102225779 A CN 102225779A
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Abstract
The invention discloses a high-pressure dissolution system and a method for bauxite, relating to the technical field of alumina production based on a Bayer method. The system comprises a multi-tube unit, an autoclave unit and a flash drum unit, wherein the multi-tube unit is connected with the autoclave unit and the flash drum unit and the autoclave unit is connected with the flash drum unit. The method comprises the steps of: conveying raw ore slurry to the multi-tube unit through a diaphragm pump and preheating to 220 DEG C; conveying the preheated ore slurry to the autoclave unit, heating to 260 DEG C, generating dissolution ore slurry through dissolution reaction, then introducing the dissolution ore slurry to the flash tank unit; and evaporating and cooling the dissolution ore slurry in the flash tank unit to 120 DEG C and introducing into a dilution tank Tt101 for dilution. Compared with traditional schemes, the high-pressure dissolution system and method for bauxite can improve production capacity, increase hourly charging amount to 600 m<3>, lower energy consumption per unit production, simplify the operation steps and reduce the repair and maintenance workload.
Description
Technical field
The present invention relates to the Bayer process technical field of alumina production, particularly a kind of bauxite pressure digestion system and method.
Background technology
The core technology scheme of the French Bi Sinie technology pressure digestion system that aluminium company introduces in 1988 is: raw pulp delivers into first pulse buffer Tp101 by high-pressure diaphragm pump, enter continuous 6 grades of single double-tube heat exchanger Ra101～106 again, the secondary steam that adopts corresponding stripping slurry flash drum to produce is preheating to 165 ℃, enter second pulse buffer Tp102 then, enter continuous 4 grades of preheating autoclave Ra107-112 (wherein 4 operations again, 2 standby), the secondary steam that adopts corresponding stripping slurry flash drum to produce is preheating to 210-220 ℃, enter continuous 7 grades of live steams heating autoclave Ra113-122 (wherein 7 operations again, 3 are standby) ore pulp further is heated to 260 ℃, enter continuous 3 order reactions at last and stop autoclave Ra123-125, the slip of finishing reaction is called stripping slurry, again by continuous 10 grades of slip flash drum Nt112-101 (wherein 10 operations, 2 are standby) evaporative cooling to 120 ℃, enter the primary wash liquor mixed diluting that dilution trap and sedimentation operation send here again and behind finite concentration, send into next operation.Wherein, the secondary steam of slip flash drum is used to heat corresponding single sleeve pipe and preheating autoclave.
The defective of this technical scheme is the maximum 500m of system feeding amount
3/ h, production capacity is lower, unit output energy consumption height.In addition, also there is following defective in this scheme: because the preheating autoclave Ra107-112 that adopts the high band of cost to stir, invest very greatly, running cost is higher; The system pipeline bore is less than normal, has limited the further maximization of system; The thermo-efficiency of 6 grades of single double-tube heat exchanger Ra101～106 is on the low side, and energy consumption is higher; Pulse buffer Tp101/Tp102 needs High Pressure Air Compressor and assists, system complex, and the Operation and Maintenance workload is very big.
Summary of the invention
(1) technical problem that will solve
The technical problem to be solved in the present invention is: how to provide a kind of inlet amount higher, production capacity is higher, more energy-conservation bauxite pressure digestion system and method.
(2) technical scheme
For solving the problems of the technologies described above, the invention provides a kind of bauxite pressure digestion system, this system comprises: many sleeve pipes unit 100, autoclave unit 200 and flash drum unit 300;
Described many sleeve pipes unit 100 connects described autoclave unit 200 and flash drum unit 300;
Described autoclave unit 200 also connects described flash drum unit 300.
Preferably, described system also comprises surge pump and dilution trap;
Described surge pump connects described many sleeve pipes unit 100;
Described dilution trap connects described flash drum unit 300.
Preferably, described many sleeve pipes unit 100 is the quadruplet pipe, it comprises 1～9 grade of quadruplet pipe Ra101～109 that is cascaded, every grade of quadruplet pipe is divided into 4 journeys, every journey 80m, every journey comprises pipe in 1 outer tube and built-in 4 arranged side by side, and interior pipe specification is ф 168 * 9mm, and the outer tube specification is ф 530 * 10mm.
Preferably, described 7～9 grades of quadruplet pipe Ra107～109 also are furnished with standby quadruplet pipe Ra107b, Ra108b and Ra109b respectively accordingly.
Preferably, described flash drum unit 300 comprises 10 grades of flash drum Nt110～101 that are cascaded, and the charge tube specification of back 3 grades of flash drum Nt103～101 is ф 356 * 14mm.
Preferably, the secondary steam pipe of 9 grades of flash drums in described 10 grades of flash drum Nt110～101 and the outer tube of described 1～9 grade of quadruplet pipe Ra101～109 connect one to one respectively.
Preferably, described autoclave unit 200 comprises two groups of autoclaves, and every group of autoclave comprises many autoclaves that are cascaded, and described two groups of autoclave quantity that autoclave comprised are identical or differ one.
Preferably, the span of the autoclave quantity n that comprises of described autoclave unit 200 is 16≤n≤24.
The present invention also provides a kind of method of using described bauxite pressure digestion system, and the method comprising the steps of:
S100: raw pulp is delivered to many sleeve pipes unit 100 by surge pump, and being preheated is 220 ℃ ore pulp;
S200: described ore pulp is heated to 260 ℃ after being transported to autoclave unit 200, and stripping reaction back generates stripping slurry and flows into flash drum unit 300;
S300: described stripping slurry enters dilution trap and dilutes behind described flash drum unit 300 evaporative coolings to 120 ℃.
Preferably, among the described step S300, described stripping slurry is used for the preheating of described step S100 to raw pulp at the secondary steam that described flash drum unit 300 evaporative cooling processes produce.
(3) beneficial effect
Bauxite pressure digestion system of the present invention and method are compared with traditional scheme, and production capacity improves, and per hour inlet amount is increased to 600m
3, the unit output energy consumption reduces, and operation steps is simplified, and the repair and maintenance workload reduces.
Description of drawings
Fig. 1 is the technological layout of traditional bauxite pressure digestion system;
Fig. 2 is the technological layout of the described bauxite pressure digestion system of the embodiment of the invention;
Fig. 3 is the method flow diagram of the described bauxite pressure digestion system of the embodiment of the invention.
Embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in further detail.Following examples are used to illustrate the present invention, but are not used for limiting the scope of the invention.
Fig. 2 is the technological layout of the described bauxite pressure digestion system of the embodiment of the invention.As shown in Figure 2, this system comprises: two surge pump Pd101～102, many sleeve pipes unit 100, autoclave unit 200, flash drum unit 300 and dilution trap Tt101 (supporting condensate system will not be described at this).
Described two surge pump Pd101～102 connect described many sleeve pipes unit 100 simultaneously, are used for raw pulp is flowed to described many sleeve pipes unit 100.
Described many sleeve pipes unit 100 connects described autoclave unit 200 and flash drum unit 300, after its secondary steam that adopts described flash drum unit 300 to emit carries out preheating to ore pulp, described ore pulp is delivered to described autoclave unit 200.Described many sleeve pipes unit 100 is the quadruplet pipe, comprises 1～9 grade of quadruplet pipe Ra101～109 that is cascaded, and every grade of quadruplet pipe comprises 4 journeys, every Cheng Changdu 80m, comprise pipe in 4 that outer tube and outer tube inside is set up in parallel, interior pipe specification is ф 168 * 9mm, and the outer tube specification is ф 530 * 10mm.Interior pipe inside is used to walk slip, is used to walk steam between interior pipe and the outer tube, so that heat exchange.Pipe specification ф 273 * 10mm in traditional single sleeve pipe heat exchange scheme, by comparison, every grade of quadruplet pipe of this programme comprises pipe in 4, its heat interchanging area increases to about 600m
2, heat exchange efficiency obviously improves.Wherein, 7～9 grades of quadruplet pipe Ra107～109 also are furnished with standby quadruplet pipe Ra107b, Ra108b and Ra109b respectively accordingly.The specification of described standby quadruplet pipe Ra107b, Ra108b and Ra109b is identical with the specification of described 1～9 grade of quadruplet pipe Ra101～109, and Ra107-109 carries out 3 grades of standby patterns of 3 grades of operation, clears up outward to realize line, has reduced the Hand scarf time.This many sleeve pipes unit also can adopt three-casing structure.
Described autoclave unit 200 connects described flash drum unit 300, and it adopts live steam that described ore pulp is heated, and described ore pulp is subjected to generate stripping slurry and be exported to described flash drum unit 300 after the thermal response.Described live steam is meant 295 ℃ of steam of the 6.0MPa that the steam-out (SO) source is supplied with.Described autoclave unit 200 comprises two groups of autoclaves, and first group of autoclave comprises 9 autoclave Ra107～Ra115 that are cascaded, and second group of autoclave comprises 10 autoclave Ra116～Ra125 that are cascaded.The ore pulp that comes out from sleeve pipe Ra109 more than the 9th grade divides two stocks not enter described two groups of autoclaves, is heated to 260 ℃ temperature of reaction with live steam, and reacted stripping slurry enters described flash drum unit 300 from the outlet interflow of two groups of autoclaves.
The autoclave total quantity is decided by the heating-surface area and the reaction time of system's needs in the described autoclave unit 200, can be 16-24 platform any amount
Described flash drum unit 300 is used for described stripping slurry is carried out evaporative cooling, and the secondary steam that the evaporative cooling process produces is exported to described many sleeve pipes unit 100.Described flash drum unit comprises 10 grades of flash drum Nt110～101 that are cascaded, and the charge tube specification of back 3 grades of flash drum Nt103～101 is ф 356 * 14mm, to meet 600m
3The inlet amount of/h.The secondary steam pipe of 9 grades of flash drum Nt110～102 in described 10 grades of flash drum Nt110～101 and the outer tube of described 1～9 grade of quadruplet pipe Ra101～109 connect one to one respectively, to realize reclaiming the secondary steam of described 9 grades of flash drum Nt110～102, to be used for the preheating of 100 pairs of ore pulps of described many sleeve pipes unit.The secondary steam that remaining 1 grade of flash drum Nt101 produces also is recovered, and is used for other operation.
Described dilution trap Tt101 connects described flash drum unit 300, is used for the flash distillation slip that described flash drum unit 300 is discharged is diluted.Dilute the primary wash liquor that used diluent produces for the subsequent sedimentation operation.
Fig. 1 is the technological layout of traditional bauxite pressure digestion system.Comparison diagram 1 and Fig. 2 are as can be known, by adopting many sleeve pipes unit 100 to replace traditional single double-tube heat exchanger Ra101～106, and change the charge tube specification of back 3 grades of flash drum Nt103～101 into ф 356 * 14mm accordingly, the inlet amount of the described bauxite pressure digestion system of the embodiment of the invention obviously improves, and the unit output energy consumption obviously reduces.The described bauxite pressure digestion system of the embodiment of the invention is after certain alumina producer is implemented, and its inlet amount is by original 470m
3/ h is increased to 600m
3/ h, the aluminum oxide annual production improves 100,000 tons.And the described bauxite pressure digestion system of embodiment of the invention operation factor reaches 95%, and the stripping temperature keeps greater than 265 ℃, and greater than 50 minutes, solubility rate was greater than 95% relatively at the reaction time of described autoclave unit 200 for ore pulp.Owing to reduced pulse buffer, air compressor machine and standby flash drum, the operation maintenance workload reduces greatly, and normal operation only needs 2 people to patrol and examine operation, and each parking maintenance only needs 40-50 people, about 24 hours of each parking maintenance.
Fig. 3 is the method flow diagram of the described aluminum oxide pressure digestion system of the embodiment of the invention, and as shown in Figure 3, the method comprising the steps of:
S100: raw pulp is delivered to many sleeve pipes unit 100 by two surge pump Pd101～102, and being preheated is 220 ℃ ore pulp;
S200: described ore pulp is heated to 260 ℃ after being transported to autoclave unit 200, and stripping reaction back generates stripping slurry and flows into flash drum unit 300;
S300: described stripping slurry enters dilution trap Tt101 and dilutes behind described flash drum unit 300 evaporative coolings to 120 ℃.
Among the described step S300, described stripping slurry is used for the preheating of described step S100 to raw pulp at the secondary steam that described flash drum unit 300 evaporative cooling processes produce.
This method flow is compared with traditional scheme, and production capacity improves, and per hour inlet amount is increased to 600m
3, operation steps is simplified, and the repair and maintenance workload reduces.
Above embodiment only is used to illustrate the present invention; and be not limitation of the present invention; the those of ordinary skill in relevant technologies field; under the situation that does not break away from the spirit and scope of the present invention; can also make various variations and modification; therefore all technical schemes that are equal to also belong to category of the present invention, and scope of patent protection of the present invention should be defined by the claims.
Claims (10)
1. a bauxite pressure digestion system is characterized in that, this system comprises: many sleeve pipes unit (100), autoclave unit (200) and flash drum unit (300);
Described many sleeve pipes unit (100) connects described autoclave unit (200) and flash drum unit (300);
Described autoclave unit (200) also connects described flash drum unit (300).
2. bauxite pressure digestion system as claimed in claim 1 is characterized in that described system also comprises surge pump and dilution trap;
Described surge pump connects described many sleeve pipes unit (100);
Described dilution trap connects described flash drum unit (300).
3. bauxite pressure digestion system as claimed in claim 2, it is characterized in that, described many sleeve pipes unit (100) is the quadruplet pipe, it comprises 1～9 grade of quadruplet pipe Ra101～109 that is cascaded, every grade of quadruplet pipe is divided into 4 journeys, every journey 80m, and every journey comprises pipe in 1 outer tube and built-in 4 arranged side by side, interior pipe specification is ф 168 * 9mm, and the outer tube specification is ф 530 * 10mm.
4. bauxite pressure digestion system as claimed in claim 3 is characterized in that, described 7～9 grades of quadruplet pipe Ra107～109 also are furnished with standby quadruplet pipe Ra107b, Ra108b and Ra109b respectively accordingly.
5. bauxite pressure digestion system as claimed in claim 3 is characterized in that, described flash drum unit (300) comprises 10 grades of flash drum Nt110～101 that are cascaded, and the charge tube specification of back 3 grades of flash drum Nt103～101 is ф 356 * 14mm.
6. bauxite pressure digestion system as claimed in claim 5 is characterized in that, the secondary steam pipe of 9 grades of flash drums in described 10 grades of flash drum Nt110～101 and the outer tube of described 1～9 grade of quadruplet pipe Ra101～109 connect one to one respectively.
7. bauxite pressure digestion system as claimed in claim 2, it is characterized in that, described autoclave unit (200) comprises two groups of autoclaves, and every group of autoclave comprises many autoclaves that are cascaded, and described two groups of autoclave quantity that autoclave comprised are identical or differ one.
8. bauxite pressure digestion system as claimed in claim 7 is characterized in that, the span of the autoclave quantity n that described autoclave unit (200) comprises is 16≤n≤24.
9. method of using each described bauxite pressure digestion system in the claim 1 to 8 is characterized in that the method comprising the steps of:
S100: raw pulp is delivered to many sleeve pipes unit (100) by surge pump, and being preheated is 220 ℃ ore pulp;
S200: described ore pulp is heated to 260 ℃ after being transported to autoclave unit (200), and stripping reaction back generates stripping slurry and flows into flash drum unit (300);
S300: described stripping slurry enters dilution trap and dilutes behind described flash drum unit (300) evaporative cooling to 120 ℃.
10. method as claimed in claim 9 is characterized in that, among the described step S300, described stripping slurry is used for the preheating of described step S100 to raw pulp at the secondary steam that described flash drum unit (300) evaporative cooling process produces.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2011101211504A CN102225779A (en) | 2011-05-11 | 2011-05-11 | High-pressure dissolution system and method for bauxite |
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| CN2011101211504A CN102225779A (en) | 2011-05-11 | 2011-05-11 | High-pressure dissolution system and method for bauxite |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103159239A (en) * | 2011-12-08 | 2013-06-19 | 贵阳铝镁设计研究院有限公司 | Heating method and apparatus of alumina dissolution sleeve |
| CN110937617A (en) * | 2019-12-27 | 2020-03-31 | 贵阳铝镁设计研究院有限公司 | Method for dissolution and evaporation combined process of Bayer process alumina plant |
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| CN101693547A (en) * | 2009-09-27 | 2010-04-14 | 杭州锦江集团有限公司 | Dissolution system |
| CN101767806A (en) * | 2008-12-31 | 2010-07-07 | 东北大学设计研究院（有限公司） | Dissolving-out process for large-sized pipeline remaining tank of diasporite bauxite ore |
| CN201634445U (en) * | 2010-01-12 | 2010-11-17 | 杭州锦江集团有限公司 | Alumina tube digestion device |
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Patent Citations (5)
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| CN1730397A (en) * | 2005-07-18 | 2006-02-08 | 贵阳铝镁设计研究院 | Method for arranging dissolving-out cannula primary heater in small scale aluminum oxide factory |
| CN101665259A (en) * | 2008-09-02 | 2010-03-10 | 中铝国际技术发展有限公司 | Ore pulp heat exchange method and system |
| CN101767806A (en) * | 2008-12-31 | 2010-07-07 | 东北大学设计研究院（有限公司） | Dissolving-out process for large-sized pipeline remaining tank of diasporite bauxite ore |
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| CN201634445U (en) * | 2010-01-12 | 2010-11-17 | 杭州锦江集团有限公司 | Alumina tube digestion device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103159239A (en) * | 2011-12-08 | 2013-06-19 | 贵阳铝镁设计研究院有限公司 | Heating method and apparatus of alumina dissolution sleeve |
| CN110937617A (en) * | 2019-12-27 | 2020-03-31 | 贵阳铝镁设计研究院有限公司 | Method for dissolution and evaporation combined process of Bayer process alumina plant |
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Application publication date: 20111026 |