CN107915243A - The hybrid technique equipment and its technological process of evaporation and twin driving composition - Google Patents
The hybrid technique equipment and its technological process of evaporation and twin driving composition Download PDFInfo
- Publication number
- CN107915243A CN107915243A CN201711485261.7A CN201711485261A CN107915243A CN 107915243 A CN107915243 A CN 107915243A CN 201711485261 A CN201711485261 A CN 201711485261A CN 107915243 A CN107915243 A CN 107915243A
- Authority
- CN
- China
- Prior art keywords
- evaporator
- evaporation
- flash device
- hybrid technique
- dissolution
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000001704 evaporation Methods 0.000 title claims abstract description 45
- 230000008020 evaporation Effects 0.000 title claims abstract description 34
- 239000000203 mixture Substances 0.000 title claims abstract description 15
- 238000010237 hybrid technique Methods 0.000 title claims abstract description 14
- 238000000034 method Methods 0.000 title claims abstract description 11
- 238000004090 dissolution Methods 0.000 claims abstract description 29
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000004519 manufacturing process Methods 0.000 claims abstract description 16
- 239000012452 mother liquor Substances 0.000 claims abstract description 12
- 238000004131 Bayer process Methods 0.000 claims abstract description 9
- 206010039509 Scab Diseases 0.000 claims abstract description 5
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 5
- 230000000694 effects Effects 0.000 claims description 33
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- 229910001679 gibbsite Inorganic materials 0.000 claims description 10
- 229910001570 bauxite Inorganic materials 0.000 claims description 8
- 229910001648 diaspore Inorganic materials 0.000 claims description 8
- 239000002002 slurry Substances 0.000 claims description 8
- 230000029087 digestion Effects 0.000 claims description 7
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000002386 leaching Methods 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 4
- 229910001593 boehmite Inorganic materials 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 239000004615 ingredient Substances 0.000 claims description 2
- 238000000926 separation method Methods 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims 1
- 230000005494 condensation Effects 0.000 claims 1
- 238000001816 cooling Methods 0.000 claims 1
- 230000007423 decrease Effects 0.000 claims 1
- 238000010025 steaming Methods 0.000 claims 1
- 230000009286 beneficial effect Effects 0.000 abstract description 3
- 230000005764 inhibitory process Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 3
- 229910052782 aluminium Inorganic materials 0.000 description 3
- 239000004411 aluminium Substances 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 238000007630 basic procedure Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000004575 stone Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000000262 chemical ionisation mass spectrometry Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Inorganic Chemistry (AREA)
- Paper (AREA)
Abstract
Evaporated and the hybrid technique equipment of twin driving composition and its technological process the invention discloses a kind of, it is to be combined together the evaporation in aluminium oxide Bayer process production system and the big steam consumption system of dissolution two, establish a new heat balance system, to obtain relatively succinct flow, and it can reduce investment outlay, beneficial to the production of full factory, the simplification of control system, mother liquor scale inhibition reagent is coordinated to scab using nothing, reliable, section vapour more efficient compared with the prior art.
Description
Technical field
The present invention relates to the evaporation-dissolution mixture length and its equipment of a kind of producing aluminium oxide by bayer, belong to aluminium oxide
Production technical field.
Background technology
In the technological process of producing aluminium oxide by bayer, digestion workshop and liquor evaporating plant are two wherein critically important works
Section.Wherein digestion workshop is responsible for leaching Al in bauxite2O3, main Leach reaction occurs herein, different ore types institute
Need the temperature that heats different, the order of required temperature from low to high is followed successively by gibbsite, boehmite, a hydraulic aluminium
Stone, is respectively 145 DEG C or so, 220 DEG C or so, 260 DEG C or so.Due to needing to save energy consumption as far as possible in industrialized production,
Therefore in Bayer process production, in order to reduce the consumption of initial steam, prior art digestion workshop and liquor evaporating plant must be to secondary
Steam is efficiently used, and coordinates preheater to form complex flow, especially using the high temperature dissolution of diaspore as most, three
The dissolution flow of diaspore is slightly simpler.
Gibbsite dissolution general flow chart such as Fig. 2 of the prior art, three stages of flashing, three-level preheating, the heating of level-one initial steam.
The dissolution flow of diaspore then needs ten grades of flash distillations or so, approximate with the flow of gibbsite in principle.
In the prior art due to need to ensure each preheater of dissolution, initial steam heater have higher heat transfer efficiency, it is necessary to
Ore pulp before dissolution is subjected to atmospheric silicon removing, is scabbed in order to avoid the low temperature silicon in ore is separated out in each preheater tube wall of dissolution, so that right
Heat transfer efficiency has a negative impact, therefore usually needs before dissolution to set up another atmospheric silicon removing workshop, such as Fig. 3 institutes
Show.
The liquor evaporating plant of the prior art, which is then mainly responsible for, evaporates the excessive moisture brought into the circulation of whole Baeyer, so that
Alkali in whole flow process can circulate.What whole Baeyer was circulated in the workshop establishes critically important, it is necessary to by decomposition nut liquid inspissation extremely
The alkali concn needed.In the prior art, countercurrent evaporation is highly developed, and the whole system thermal efficiency, running rate are all higher, and operation is steady
Fixed, environment is clean and tidy, by taking sextuple-effect evaporation as an example, its basic procedure such as Fig. 4.
Current technology all comparative maturities, but process CIMS is complicated, and equipment is more, and configuration is taken up an area.By simulating and calculating, look for
To a kind of more succinct, energy saving, and also very reliable flow is extremely necessary.
The content of the invention
The hybrid technique equipment formed with twin driving and its technological process are evaporated the object of the present invention is to provide a kind of,
With overcome the deficiencies in the prior art.
Technical scheme is as follows：
The present invention is the hybrid technique equipment of such a evaporation and twin driving composition, it is by aluminium oxide Bayer process
The big steam consumption system of evaporation and dissolution two in production system is combined together, and establishes a new heat balance system；Wherein,
Vapo(u)rization system is condensed by 1st effective evaporator, 2nd effect evaporator, triple effect evaporator, last evaporator and water cooler, and secondary vapour
First and second vapour condensate water self-evaporating device two of water flash-pot, secondary vapour condensate water self-evaporating device three form, initial steam heater with
Digester, primary flash device and two-stage flash device composition digestion series, two systems are interrelated, collectively form a thermal balance
System.
Wherein, last evaporator connection water cooler, meanwhile, last evaporator connection triple effect evaporator, triple effect evaporator connects
2nd effect evaporator, 2nd effect evaporator connection 1st effective evaporator are connect, 1st effective evaporator connects heater, and heater connects digester,
Digester connects primary flash device, primary flash device connection two-stage flash device；Heater connection live steam condensed water flash vessel, one
Imitate evaporator and connect secondary vapour condensed water flash device one, 2nd effect evaporator connects secondary vapour condensed water flash device two, triple effect evaporation
Device connects secondary vapour condensed water flash device three.
Further, the either number of devices of vapo(u)rization system or digestion series equipment, can be according to actual dissolution
Temperature is needed and increased and decreased.
The invention also provides the evaporation using the equipment and the hybrid technique flow of twin driving composition, which uses
In the Bayer process production of diaspore, boehmite and gibbsite, which is to be based on the said equipment by oxygen
Change the evaporation in aluminium Bayer process production system and the big steam consumption system of dissolution two is combined together, establish a new thermal balance
System, to obtain relatively succinct flow, and can reduce investment outlay, and beneficial to the production of full factory, the simplification of control system, coordinate mother liquor resistance
Dirty reagent is scabbed using nothing, reliable, section vapour more efficient compared with the prior art.The flow can be used for diaspore, a water soft
In the Bayer process production technology of aluminium stone and gibbsite.Described by taking the low temperature dissolution flow of gibbsite as an example.Concrete technology stream
Journey is as follows：Vaporizing raw liquor is divided into two parts, and most of stoste enters vapo(u)rization system from four-effect evaporator (or last evaporator), few
Partial stoste and bauxite mixed ingredients, so that mixing is solid containing 800g/L or so is reached, convey easy to ore slurry pump.Into evaporation
The mother liquor of device 4 no longer flashes after triple effect evaporator, 2nd effect evaporator and 1st effective evaporator countercurrent evaporation, and it is new to be directly entered dissolution
Steam heater, mixes after being heated to sufficiently high temperature with the high concentration bauxite slurry of low temperature, is carried out into digester main
Chemical reaction, initial steam heater come out mother liquor temperature depend on digester come out dissolution after slurry temperature, this is sentenced
Exemplified by gibbsite, slurry temperature is 145 DEG C or so after dissolution, and mother liquor temperature requires heat to 193 DEG C or so.Ore pulp after dissolution
Into primary flash device, mixed after lightening the indirect steam purification come with live steam condensed water indirect steam, as an effect evaporation
The source of the gas of device, the ore pulp that primary flash device comes out go successively to two-stage flash device, then go to next workshop section.The two of two-stage flash device
The secondary vapour come out after secondary vapour purification with 1st effective evaporator separation chamber mixes, the heating source of the gas as 2nd effect evaporator.Water cooler
Negative pressure source is provided for whole system.Whole flow process mother liquor obtains relatively independent heating, can be prevented with the use of fiting chemical reagent
The generation only to scab.
The invention has the advantages that：
(1) it is simple to be handled for a workshop by the original main flow problem for needing three workshops to solve, flow is simplified,
Reduce investment outlay cost, industrialized production is more reasonable.
(2) coordinating prevents the chemical reagent of spent liquor scaling from using, and all heat transfer units remove the puzzlement that scabs from, and heat transfer efficiency is more
Height, running rate higher, is extremely beneficial to production.
(3) working condition is flexible and changeable, for example evaporation volume needs to change so as to cause steam demand amount to change
When, steam consumption quantity can be adjusted indirectly into the flow of vapo(u)rization system by adjusting evaporation mother liquor, so that production is stablized, or
Initial steam is added in vapo(u)rization system reserve steam mouth to meet the uncontrollable requirement of production.
(4) for the flow compared with the flow that three workshops of the prior art form, steam consumption is lower slightly, more economically, runs into
This is lower.
(5) come compared with the prior art, floor space is reduced significantly.
Brief description of the drawings
Fig. 1 is the process flow chart of the present invention；
Fig. 2 is the gibbsite dissolution general flow chart of the prior art；
Fig. 3 is the atmospheric silicon removing workshop schematic diagram of the prior art；
Fig. 4 is the sextuple-effect evaporation basic procedure schematic diagram of the prior art.
Description of reference numerals：1- 1st effective evaporators, 2- 2nd effect evaporators, 3- triple effect evaporators, 4- last evaporators, 5- water
Cooler, bis- vapour condensate water self-evaporating devices one of 6-, bis- vapour condensate water self-evaporating devices two of 7-, bis- vapour condensate water self-evaporating devices of 8-
Three, 9- heater, 10- digesters, 11- primary flash devices, 12- two-stage flash devices, 13- live steam condensed water flash vessels.
Embodiment
The invention will be further described with reference to the accompanying drawings and examples, but not as any limitation of the invention.
Embodiment 1：
As shown in Figure 1, evaporation flow and twin driving technique are combined by the present invention, with the low temperature dissolution of gibbsite
Exemplified by, such as Fig. 1.For vaporizing raw liquor in addition to ore grinding part is participated in, remaining fully enters the last evaporator 4 of evaporation section, carries out inverse
Flow evaporator, through triple effect evaporator 3,2nd effect evaporator 2, after being come out to 1st effective evaporator 1, no longer flashes, is directly entered dissolution portion
The initial steam heater 9 divided, after being heated to the temperature needed for follow-up digester 10, mixes with low temperature large arch dam bauxite slurry, arrives
Up to dissolution required temperature, stopped into digester 10, the alumina leaching in bauxite is entered in solution.After dissolution ore pulp into
Enter primary flash device 11, control the saturation reheat steam temperature degree of the primary flash device 11 to meet the temperature of vapo(u)rization system gas and use
Tolerance requirement, aforementioned evaporation system do not add initial steam, using the secondary secondary vapour of vapour and initial steam of primary flash device 11 as
Source of the gas, the initial steam flow (chain-dotted line part) of vapo(u)rization system shown in figure are used as startup or case of emergency.From level-one
The ore pulp that flash vessel 11 comes out goes successively to two-stage flash device 12 and cools down and lighten secondary vapour use for 2nd effect evaporator 2, with must
To both economical energy consumption index.Finished product dissolved mineral slurry is just obtained after being come out from two-stage flash device 12.
The flow only heats mother liquor, make mother liquor temperature be increased to after required temperature again enter digester 10 before with it is low
Warm ore pulp mixing.Since the heating target of whole system is liquid, rather than the ore pulp rich in bauxite ore particles, thus it is all plus
The heat transfer efficiency of hot device 9 is very high, and since no bauxite ore particles wash away heat transfer tube wall, the longevity of institute's having heaters 9
Life greatly improves, therefore the running rate of whole system is higher than the prior art., can due to no longer worrying the problem of preheater scabs
To save pre-desiliconizing workshop (such as Fig. 3).
In the flow, the temperature of dissolution is depended on using the effect number of evaporation flow.When leaching condition changes, dissolution temperature
When degree requires higher, evaporation flow can use more effect numbers.
When a water is soft or diaspore uses the flow, since leaching temperature greatly improves, it is thus possible to using six
The effect even flow of seven effects or even more multiple-effect, the steam consumption can be lower, can be shown relative to the more preferable business efficiency of former technology, and
And the effect number of evaporation section is mainly dependent on the evaporation volume of full factory at that time.Flow under these operating modes, with this flow chart principle
Equally, from the limitation of this flow chart, it is covered by within the present invention.
It is the concrete application example of the present invention above, the present invention also has others embodiments, all to use equivalent substitution
Or the technical solution that equivalent transformation is formed, all fall within protection domain of the presently claimed invention.
Claims (8)
- A kind of 1. hybrid technique equipment evaporated and twin driving forms, it is characterised in that：Aluminium oxide Bayer process is produced and is The big steam consumption system of evaporation and dissolution two in system is combined together, and establishes a new heat balance system；Wherein, evaporation system System is by 1st effective evaporator (1), 2nd effect evaporator (2), triple effect evaporator (3), last evaporator (4) and water cooler (5), and two Secondary vapour condensate water self-evaporating device one (6), secondary vapour condensate water self-evaporating device two (7), secondary three (8) group of vapour condensate water self-evaporating device Into, initial steam heater (9) and digester (10), primary flash device (11) and two-stage flash device (12) composition digestion series, two A system is interrelated, collectively forms a heat balance system.
- 2. evaporation according to claim 1 and the hybrid technique equipment of twin driving composition, it is characterised in that：The end Evaporator (4) connection water cooler (5) is imitated, meanwhile, last evaporator (4) connection triple effect evaporator (3), triple effect evaporator (3) is even 2nd effect evaporator (2) is connect, 2nd effect evaporator (2) connection 1st effective evaporator (1), 1st effective evaporator (1) connection heater (9), adds Hot device (9) connection digester (10), digester (10) connection primary flash device (11), primary flash device (11) connection two-stage flash Device (12)；Heater (9) connection live steam condensed water flash vessel (13), 1st effective evaporator (1) connect secondary vapour condensed water flash Device one (6), 2nd effect evaporator (2) connect secondary vapour condensed water flash device two (7), and triple effect evaporator (3) connects secondary vapour condensation Water flash vessel three (8).
- 3. evaporation according to claim 1 and the hybrid technique equipment of twin driving composition, it is characterised in that：Either The number of devices of vapo(u)rization system or digestion series equipment, needs and increases and decreases all in accordance with actual leaching temperature.
- 4. a kind of evaporation of equipment using described in claim 1 and the hybrid technique flow of twin driving composition, the flow For in the Bayer process production of diaspore, boehmite and gibbsite, it is characterised in that the technological process is used for three Include the following steps during the Bayer process production of diaspore：Vaporizing raw liquor is divided into two parts, and most of stoste is from last evaporator (4) Into vapo(u)rization system, least a portion of stoste and bauxite mixed ingredients,；Into last evaporator (4) mother liquor through triple effect evaporation No longer flashed after device (3), 2nd effect evaporator (2) and 1st effective evaporator (1) countercurrent evaporation, be directly entered dissolution initial steam heater (9), mixed after being heated to sufficiently high temperature with the high concentration bauxite slurry of low temperature, main change is carried out into digester (10) Reaction is learned, the mother liquor temperature that initial steam heater (9) comes out depends on slurry temperature after the dissolution that digester (10) comes out；Dissolution Ore pulp enters primary flash device (11) afterwards, mixes, makees with live steam condensed water indirect steam after lightening the indirect steam purification come For the source of the gas of 1st effective evaporator (1), the ore pulp that primary flash device (11) comes out goes successively to two-stage flash device (12), under then going One workshop section.
- 5. evaporation according to claim 4 and the hybrid technique flow of twin driving composition, it is characterised in that：Two level is dodged The secondary vapour come out after the secondary vapour purification of steaming device (12) with 1st effective evaporator (1) separation chamber mixes, as 2nd effect evaporator (2) Heating source of the gas.
- 6. evaporation according to claim 4 and the hybrid technique flow of twin driving composition, it is characterised in that：With water cooling Device (5) provides negative pressure source for whole system.
- 7. evaporation according to claim 4 and the hybrid technique flow of twin driving composition, it is characterised in that：Whole stream Journey mother liquor obtains relatively independent heating.
- 8. evaporation according to claim 4 and the hybrid technique flow of twin driving composition, it is characterised in that：With combination Learning the use of reagent prevents the generation to scab.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711485261.7A CN107915243A (en) | 2017-12-30 | 2017-12-30 | The hybrid technique equipment and its technological process of evaporation and twin driving composition |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711485261.7A CN107915243A (en) | 2017-12-30 | 2017-12-30 | The hybrid technique equipment and its technological process of evaporation and twin driving composition |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107915243A true CN107915243A (en) | 2018-04-17 |
Family
ID=61894571
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201711485261.7A Pending CN107915243A (en) | 2017-12-30 | 2017-12-30 | The hybrid technique equipment and its technological process of evaporation and twin driving composition |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107915243A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
| CN112684772A (en) * | 2020-12-31 | 2021-04-20 | 贵阳振兴铝镁科技产业发展有限公司 | Thermal balance control system and method for dissolving out aluminum oxide |
| CN117069130A (en) * | 2023-07-12 | 2023-11-17 | 沈阳铝镁设计研究院有限公司 | Method for reducing new steam consumption in alumina production |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102381721A (en) * | 2010-09-02 | 2012-03-21 | 沈阳铝镁设计研究院有限公司 | Method for processing diaspore ore to produce alumina |
| CN104098117A (en) * | 2013-04-12 | 2014-10-15 | 沈阳铝镁设计研究院有限公司 | High-pressure dissolution-out and evaporation combined energy-saving method in production of aluminium oxide |
| CN105692665A (en) * | 2016-03-17 | 2016-06-22 | 东北大学设计研究院（有限公司） | Parallel row tube and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN208667120U (en) * | 2017-12-30 | 2019-03-29 | 贵阳铝镁设计研究院有限公司 | The hybrid technique equipment of evaporation and twin driving composition |
-
2017
- 2017-12-30 CN CN201711485261.7A patent/CN107915243A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102381721A (en) * | 2010-09-02 | 2012-03-21 | 沈阳铝镁设计研究院有限公司 | Method for processing diaspore ore to produce alumina |
| CN104098117A (en) * | 2013-04-12 | 2014-10-15 | 沈阳铝镁设计研究院有限公司 | High-pressure dissolution-out and evaporation combined energy-saving method in production of aluminium oxide |
| CN105692665A (en) * | 2016-03-17 | 2016-06-22 | 东北大学设计研究院（有限公司） | Parallel row tube and remaining tank dissolving-out system and method for gibbsite bauxite |
| CN208667120U (en) * | 2017-12-30 | 2019-03-29 | 贵阳铝镁设计研究院有限公司 | The hybrid technique equipment of evaporation and twin driving composition |
Non-Patent Citations (2)
| Title |
|---|
| 朱祖宝: ""双流法高压溶出过程的数据挖掘及优化技术研究"" * |
| 郭焕雄: "强化一水硬铝石矿的拜耳法溶出" * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
| CN112684772A (en) * | 2020-12-31 | 2021-04-20 | 贵阳振兴铝镁科技产业发展有限公司 | Thermal balance control system and method for dissolving out aluminum oxide |
| CN112684772B (en) * | 2020-12-31 | 2024-05-03 | 贵阳振兴铝镁科技产业发展有限公司 | Heat balance control system and method for aluminum oxide dissolution |
| CN117069130A (en) * | 2023-07-12 | 2023-11-17 | 沈阳铝镁设计研究院有限公司 | Method for reducing new steam consumption in alumina production |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107915243A (en) | The hybrid technique equipment and its technological process of evaporation and twin driving composition | |
| CN104803535B (en) | A kind of recovery system and recovery process for reclaiming salt from desulfurization wastewater | |
| CN102616973B (en) | Method and device for processing high-saline organic wastewater | |
| CN105692665B (en) | The tubulation dwell tank digestion series in parallel and method of gibbsitic bauxite | |
| CN106669207A (en) | MVR (mechanical vapor recompression) evaporation crystallization system and method for high-salinity wastewater | |
| CN106746136A (en) | The technique of zero discharge and system of a kind of desulfurization wastewater | |
| CN101445256A (en) | Stripping technique for large pipeline for monohydrate hard bauxite ore with staying tank added | |
| CN107789851A (en) | A kind of triple effect vacuum vaporation system for improving copper sulphate evaporation efficiency | |
| CN208667120U (en) | The hybrid technique equipment of evaporation and twin driving composition | |
| CN209286688U (en) | MVR evaporator replaces the Production of Barium Chloride system of traditional four-effect evaporator | |
| CN103922529A (en) | Low-energy-consumption device for recycling hydrochloric acid waste water and method for recycling hydrochloric acid waste water | |
| CN102249271B (en) | Tube array and remaining tank dissolving-out system and method for gibbsite bauxite | |
| CN102100973B (en) | Multistage evaporating process in viscose production | |
| CN205528225U (en) | Desulfurization waste water zero release processing system | |
| CN110127615A (en) | Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate | |
| CN103848864A (en) | Preparation process of high-purity triisobutyl phosphate | |
| CN102515201B (en) | Method and device for recycling waste clear liquid produced in process for producing sodium carbonate by ammonia-soda process | |
| CN105293544A (en) | Dissolution live steam condensate water evaporation secondary utilization method | |
| CN1915827B (en) | Method and equipment for vaporizing full flash distillation of sodium aluminate liquor in technique for producing alumina | |
| CN114044551B (en) | Separation tower for treating condensed water and method thereof | |
| CN106500086B (en) | A kind of exhaust steam recycling and recovery system | |
| CN206152365U (en) | Process systems of neutralization production cooling crystallization type product | |
| CN201906471U (en) | Vacuum concentration device for diluted acid | |
| CN102464346A (en) | Seven-effect falling film evaporation technology for sodium aluminate solution | |
| CN107915244A (en) | A kind of process unit and method of gibbsitic bauxite twin driving |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180417 |