CN103130253A - Two stage decomposition process method of Bayer process alumina production - Google Patents
Two stage decomposition process method of Bayer process alumina production Download PDFInfo
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- CN103130253A CN103130253A CN2011103802585A CN201110380258A CN103130253A CN 103130253 A CN103130253 A CN 103130253A CN 2011103802585 A CN2011103802585 A CN 2011103802585A CN 201110380258 A CN201110380258 A CN 201110380258A CN 103130253 A CN103130253 A CN 103130253A
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Abstract
The present invention discloses a two stage decomposition process method of Bayer process alumina production. According to the method, a fine liquid obtained from control filtration and a decomposition mother liquor are subjected to heat exchange through a plate type heat exchanger to obtain a hot fine liquid and a cold fine liquid; the hot fine liquid is mixed with filter cake of a fine seed filter to form a fine seed slurry, and the fine seed slurry is conveyed to an agglomeration segment decomposition first tank through a crystal seed pump to carry out agglomeration decomposition; the cold fine liquid is mixed with filter cake of a coarse seed filter to form a coarse seed slurry, and the coarse seed slurry is conveyed to a growth segment decomposition first tank through a crystal seed pump to carry out growth; the fine seed slurry stays for 4-6 h in the agglomeration segment decomposition first tank, is conveyed to a middle temperature reduction cooler through a submerged pump, is subjected to heat exchange with circulation water, and then enters the growth segment decomposition first tank; the treated fine seed slurry and the coarse seed slurry are continuously subjected to decomposition growth; an end washing fine seed slurry obtained from a fine seed slurry settlement tank is added; the mixed slurry is continuously subjected to decomposition growth in the decomposition first tank; and after completing decomposition growth, the submerged pump is adopted to convey the slurry to a finished product hydrocyclone to grade, and the bottom flow of the hydrocyclone is adopted as a finished product slurry.
Description
Technical field
The present invention relates to a kind of flow and method of decomposition of Bayer process alumina producing.
Background technology
Decomposition of crystal seed is one of critical process of alumina producing Bayer process, and it has great impact to the output of product and the technico-economical comparison of quality and full factory.Weighing kind of the leading indicator of minute operation effectiveness is the unit production capacity of quality, rate of decomposition and the decomposer of aluminium hydroxide.
The kind of sodium aluminate solution minute process is not that simple crystal seed is grown up, and also carries out simultaneously some other physicochemical change, and a lot of phenomenons and result of study show that the process of whole aluminium hydroxide crystallization is very complicated, comprising:
1. secondary nucleation
2. aluminum hydroxide crystals breaks and abrasion
3. aluminum hydroxide crystals grows up
4. the agglomeration of aluminum hydroxide grain
So-called agglomeration, under the effect of the power such as surface tension that form at the close contact between Van der Waals force, self-adhesion, sticking power and capillary force and material exactly, the phenomenon that links together that particulate matter is spontaneous and directed.When sodium aluminate solution decomposed under certain condition, agglomeration can be preponderated.Just should effectively utilize agglomeration mechanism for obtaining the large aluminium hydroxide of granularity, full out increase the size of lattice crystal grain when crystallization, make it meet the requirements of size.
The agglomeration of growing up with crystal grain of crystal seed causes the crystalline aluminum hydroxide chap.When factory require to produce sandy alumina, to create conditions exactly, avoid as much as possible or reduce breaking of the secondary nucleation of kind of timesharing and aluminum hydroxide grain, promote simultaneously the agglomeration with crystal grain of growing up of crystal.
Summary of the invention
The object of the invention is to: a kind of two sections decomposition process methods of Bayer process alumina producing are provided, cause the crystalline aluminum hydroxide chap, plant timesharing and form the deficiencies such as breaking of secondary nucleus, aluminum hydroxide grain with the agglomeration with crystal grain of growing up that overcomes crystal seed that prior art exists.
in order to solve described technical problem, the present invention takes following technical scheme: two sections decomposition process of the present invention comprise agglomeration section decomposition process and the section of growing up decomposition process, process is as follows: obtain hot seminal fluid and cold seminal fluid from controlled filter seminal fluid out after plate-type heat exchanger and decomposition nut liquid carry out heat exchange, hot seminal fluid with become thin seed slurries after the filter cake of thin seed filter mixes, control mixed slurry temperature at 75 ~ 80 ℃, admittedly contain 120 ~ 150g/l, be pumped into agglomeration section decomposer through crystal seed and carry out the agglomeration decomposition, cold seminal fluid is mixed into thick seed slurries with the filter cake of thick seed filter, controls mixed slurry temperature at 60 ~ 65 ℃, admittedly contain 300-450g/l, is pumped into the section of growing up decomposer through crystal seed and grows up, thin seed slurries stop in agglomeration section decomposer delivered to agglomeration section intermediate temperature drop water cooler by agglomeration section submerged pump in 4-6 hour and recirculated water carries out heat exchange, slurry temperature after heat exchange is 60 ~ 65 ℃, then enter the first groove of the section of growing up decomposer, proceed to decompose with thick seed slurries and grow up, grow up and carry out 18 ~ 22 hours, add from the thin seed slurries of the end washing that thin seed subsider comes, mixed slurries are proceeded to decompose in the section of growing up decomposer and are grown up, decompose and adopt the section of growing up intermediate temperature drop water cooler to carry out cooling to slip in the process of growing up, decompose final temperature at 48 ~ 50 ℃ to control, decompose after 30-35 hour, the employing section of growing up submerged pump carries out classification with slurry pipeline transport to finished product water spigot, the underflow of finished product water spigot is as the finished product slip, being transported to the finished product filter filters, the overflow of finished product water spigot enters thick seed swirler and carries out classification.
With the hot seminal fluid temperature that obtains after the mother liquor heat exchange be 75 ~ 80 ℃, cold seminal fluid temperature is 60 ~ 65 ℃.
Hot seminal fluid accounts for the 30-40% of total semen volume, and cold seminal fluid accounts for the 60-70% of total semen volume.
Underflow after thick seed cyclone classification is delivered to thick seed filter as thick seed slurries and is filtered, and the filter cake that obtains after filtration mixes with cold seminal fluid, delivers to the section of growing up decomposer; Thick seed swirler overflow enters the sedimentation of thin seed subsider.
Underflow after the sedimentation of meticulous seed subsider is divided into two portions, and a part is delivered to thin seed filter and filtered after thin seed washing device washing, then mix with hot seminal fluid, as the charging of agglomeration section decomposition process; Another part directly adds the medial launder of the section of growing up decomposition process without washing, the thick seed of conduct after growing up 18 ~ 22 hours.
Underflow through washing, filtration accounts for the 30-40% of underflow total amount, directly adds the underflow of the section of growing up middle portion groove to account for the 60-70% of underflow total amount without washing.
The quantity per-cent that relates in foregoing refers to weight percent.
Two sections decomposition process methods of Bayer process alumina producing of the present invention, effectively guide with the process of growing up by the agglomeration to crystal seed, thereby greatly improve granularity and the intensity of finished product aluminium hydroxide, make the quality of finished product aluminum oxide be improved, better to satisfy the requirement of subsequent disposal operation (as electrolysis), therefore obtain better selling price, for factory creates better economic benefit.
Description of drawings
Fig. 1 is schematic flow sheet of the present invention (contains through flow sheet equipment), wherein
1 - 1-1 agglomeration agglomeration segment decomposition tank exploded tank section 1-2 first agglomeration tank exploded slot end segment Slot 2 - Attached under paragraph liquid poly pump 3 - middle segment agglomeration cooling cooler 4 - grew segment segment grew decomposition tank 4-1 decomposition tank 4-2 segment grew grew up middle section finished 4-3 slots slot 5 - grew up sump pump under paragraph 6 - grow up the middle section to cool the intercooler 7 - finished water spin 8 - coarse seed water spin 9 - fine seed settling tank 10 - fine seed washing device 11 - fine seed filter machine 12 - fine seed seed slot 13 - coarse filter 14 seed - coarse seed seed slot 15 - decomposed liquor heat storage device 16 semen .
Embodiment
Embodiments of the invention:
Embodiment one: as shown in Figure 1, from controlled filter seminal fluid out, be divided into two-way and carry out heat exchange through plate-type heat exchanger, a part (30%) temperature after the plate-type heat exchanger heat exchange is at 80 ℃, become hot seminal fluid, another part (70%) is controlled temperature after its heat exchange at 65 ℃, becomes cold seminal fluid; Seed seed mixer 12 is interior becomes thin seed slurries after mixing thin for the filter cake of hot seminal fluid and thin seed filter 11, controls mixed slurry temperature at approximately 77 ℃, admittedly contain 150g/l, carries out agglomeration in crystal seed is pumped into agglomeration section decomposer 1; Cold seminal fluid is mixed into thick seed slurries with the filter cake of thick seed filter 13 in thick seed seed mixer 14, controls mixed slurry temperature at 62 ℃, admittedly contain 450g/l, is pumped into the first groove 4 of the decomposition section of growing up through crystal seed and grows up.
slip was delivered to agglomeration section intermediate temperature drop water cooler 3 by agglomeration section submerged pump 2 in 6 hours in the interior stop of agglomeration section decomposer 1 and is carried out heat exchange with recirculated water, slurry temperature after heat exchange is 60 ℃, then enter the first groove 4 of the section of growing up, proceed to decompose with thick seed slurries and grow up, carry out about 20 hours growing up, add from the thin seed slurries of the end washing of thin seed subsider 9, mixed slurries are proceeded to decompose in the section of growing up decomposer 4 and are grown up, decompose and adopt 6 pairs of slips of the section of growing up intermediate temperature drop water cooler to carry out cooling in the process of growing up, decompose final temperature at 50 ℃ to control, decompose after 32 hours, the employing section of growing up submerged pump 5 carries out classification with slurry pipeline transport to finished product water spigot 7, the underflow of finished product water spigot 7 is as the finished product slip, being transported to finished product filters, the overflow of finished product water spigot 7 enters thick seed swirler 8 and carries out classification, thick seed swirler 8 underflows are delivered to thick seed filter 13 as thick seed slurries and are filtered, the filter cake that obtains after filtration mixes with cold seminal fluid in thick seed seed mixer 14, deliver to the section of growing up decomposer 4, overflow enters thin seed subsider 9, after sedimentation after a while, the underflow of thin seed subsider 9 is divided into two portions, a part is delivered to thin seed filter 11 and is filtered after thin seed washing device 10 washings, then mix with hot clear liquid in thin seed seed mixer 12, as the agglomeration section feeding, another part adds and decomposes the section of growing up medial launder.
Embodiment two: as shown in Figure 1, from controlled filter seminal fluid out, divide two-way to carry out heat exchange through plate-type heat exchanger, a part (35%) temperature after the plate-type heat exchanger heat exchange is at 76 ℃, become hot seminal fluid, another part (65%) is controlled temperature after its heat exchange at 62 ℃, become cold seminal fluid, seed seed mixer 12 is interior becomes thin seed slurries after mixing thin for the filter cake of hot seminal fluid and thin seed filter 11, control mixed slurry temperature at approximately 75 ℃, admittedly contain 120g/l, carry out agglomeration in crystal seed be pumped into agglomeration section decomposer 1; Cold seminal fluid is mixed into thick seed slurries with the filter cake of thick seed filter 13 in thick seed seed mixer 14, controls mixed slurry temperature at 60 ℃, admittedly contain 300g/l, is pumped into the first groove 4 of the decomposition section of growing up through crystal seed and grows up.
slip was delivered to agglomeration section intermediate temperature drop water cooler 3 by agglomeration section submerged pump 2 in 6 hours in the interior stop of agglomeration section decomposer 1 and is carried out heat exchange with recirculated water, slurry temperature after heat exchange is 60 ℃, then enter the first groove 4 of the section of growing up, proceed to decompose with thick seed slurries and grow up, carry out about 20 hours growing up, add from the thin seed slurries of the end washing of thin seed subsider 9, mixed slurries 4 are proceeded to decompose and are grown up in the section of growing up decomposer, decompose and adopt 6 pairs of slips of the section of growing up intermediate temperature drop water cooler to carry out cooling in the process of growing up, decompose final temperature at 50 ℃ to control, decompose after 32 hours, the employing section of growing up submerged pump 5 carries out classification with slurry pipeline transport to finished product water spigot 7, the underflow of finished product water spigot 7 is as the finished product slip, being transported to finished product filters, the overflow of finished product water spigot 7 enters thick seed swirler 8 and carries out classification, the underflow of thick seed swirler 8 is delivered to thick seed filter 13 as thick seed slurries and is filtered, the filter cake that obtains after filtration mixes with cold seminal fluid in thick seed seed mixer 14, deliver to the section of growing up decomposer 4, overflow enters thin seed subsider 9, after sedimentation after a while, the underflow of thin seed subsider 9 is divided into two portions, a part is delivered to thin seed filter 11 and is filtered after thin seed washing device 10 washings, then mix with hot clear liquid in thin seed seed mixer 12, as the agglomeration section feeding, another part adds and decomposes the section of growing up medial launder.
Claims (6)
1. two of a Bayer process alumina producing sections decomposition process methods is characterized in that: described two sections decomposition process comprise agglomeration section and the section of growing up, process is as follows: obtain hot seminal fluid and cold seminal fluid from controlled filter seminal fluid out after plate-type heat exchanger and decomposition nut liquid carry out heat exchange, hot seminal fluid with become thin seed slurries after the filter cake of thin seed filter mixes, control mixed slurry temperature at 75 ~ 80 ℃, admittedly contain 120 ~ 150g/l, be pumped into agglomeration section decomposer (1) through crystal seed and carry out the agglomeration decomposition, cold seminal fluid is mixed into thick seed slurries with the filter cake of thick seed filter (13), controls mixed slurry temperature at 60 ~ 65 ℃, admittedly contain 300-450g/l, is pumped into the section of growing up decomposer (4) through crystal seed and grows up, thin seed slurries stop in agglomeration section decomposer delivered to agglomeration section intermediate temperature drop water cooler (3) by agglomeration section submerged pump (2) in 4-6 hour and recirculated water carries out heat exchange, slurry temperature after heat exchange is 60 ~ 65 ℃, then enter the first groove of the section of growing up decomposer, proceed to decompose with thick seed slurries and grow up, grow up and carry out 18 ~ 22 hours, add from the thin seed slurries of the end washing that thin seed subsider (9) comes, mixed slurries are proceeded to decompose in the section of growing up decomposer and are grown up, decompose and adopt the section of growing up intermediate temperature drop water cooler (6) to carry out cooling to slip in the process of growing up, decompose final temperature at 48 ~ 50 ℃ to control, decompose after 30-35 hour, the employing section of growing up submerged pump (5) carries out classification with slurry pipeline transport to finished product water spigot (7), the underflow of finished product water spigot (7) is as the finished product slip, being transported to the finished product filter filters, the overflow of finished product water spigot (7) enters thick seed swirler (8) and carries out classification.
2. two of Bayer process alumina producing according to claim 1 sections decomposition process methods is characterized in that: with the hot seminal fluid temperature that obtains after the mother liquor heat exchange be 75 ~ 80 ℃, cold seminal fluid temperature is 60 ~ 65 ℃.
3. two of Bayer process alumina producing according to claim 1 sections decomposition process methods, it is characterized in that: hot seminal fluid accounts for the 30-40% of total semen volume, and cold seminal fluid accounts for the 60-70% of total semen volume.
4. two of Bayer process alumina producing according to claim 1 sections decomposition process methods, it is characterized in that: the underflow after thick seed swirler (8) classification is delivered to thick seed filter (13) as thick seed slurries and is filtered, the filter cake that obtains after filtration mixes with cold seminal fluid, delivers to the section of growing up decomposer (4); Thick seed swirler (8) overflow enters thin seed subsider (9) sedimentation.
5. two of Bayer process alumina producing according to claim 4 sections decomposition process methods, it is characterized in that: the underflow after meticulous seed subsider (9) sedimentation is divided into two portions, a part is delivered to thin seed filter (11) and is filtered after thin seed washing device (10) washing, then mix with hot seminal fluid, as the charging of agglomeration section decomposition process; Another part directly adds the medial launder of the section of growing up decomposition process without washing, the thick seed of conduct after growing up 18 ~ 22 hours.
6. two of Bayer process alumina producing according to claim 5 sections decomposition process methods, it is characterized in that: the underflow through washing, filtration accounts for the 30-40% of underflow total amount, directly adds the underflow of the section of growing up middle portion groove to account for the 60-70% of underflow total amount without washing.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103159241A (en) * | 2011-12-15 | 2013-06-19 | 贵阳铝镁设计研究院有限公司 | Two-section decomposition process for alumina production by Bayer process |
| CN105399122A (en) * | 2015-12-18 | 2016-03-16 | 东北大学设计研究院（有限公司） | First-tank temperature controlling and discharging grading method for producing sandy aluminium oxide through two-segment decomposition |
| CN106629798A (en) * | 2016-12-29 | 2017-05-10 | 东北大学设计研究院（有限公司） | Novel two-stage-decomposition intensive system and process for producing sandy aluminum oxide |
| CN106986362A (en) * | 2017-04-12 | 2017-07-28 | 柳健康 | A kind of sodium aluminate solution high concentration is low admittedly containing one section of seeded precipitation technique |
| CN111410221A (en) * | 2020-03-26 | 2020-07-14 | 重庆市南川区先锋氧化铝有限公司 | Be applicable to crystal seed processing apparatus among sodium aluminate production technology |
| CN114264171A (en) * | 2021-12-09 | 2022-04-01 | 沈阳铝镁设计研究院有限公司 | Semen cooling device and process for two-stage decomposition |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1631786A (en) * | 2004-12-28 | 2005-06-29 | 中国铝业股份有限公司 | Process for producing sandy alumina by crystal seed decomposition |
| CN101070170A (en) * | 2007-05-30 | 2007-11-14 | 山东铝业股份有限公司 | Small two-stage method aluminium hydroxide crystal seed decomposing method |
| CN101092242A (en) * | 2007-05-22 | 2007-12-26 | 山东铝业股份有限公司 | Three stages, two seeds technique of seed crystal decomposition |
-
2011
- 2011-11-25 CN CN201110380258.5A patent/CN103130253B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1631786A (en) * | 2004-12-28 | 2005-06-29 | 中国铝业股份有限公司 | Process for producing sandy alumina by crystal seed decomposition |
| CN101092242A (en) * | 2007-05-22 | 2007-12-26 | 山东铝业股份有限公司 | Three stages, two seeds technique of seed crystal decomposition |
| CN101070170A (en) * | 2007-05-30 | 2007-11-14 | 山东铝业股份有限公司 | Small two-stage method aluminium hydroxide crystal seed decomposing method |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103159241A (en) * | 2011-12-15 | 2013-06-19 | 贵阳铝镁设计研究院有限公司 | Two-section decomposition process for alumina production by Bayer process |
| CN105399122A (en) * | 2015-12-18 | 2016-03-16 | 东北大学设计研究院（有限公司） | First-tank temperature controlling and discharging grading method for producing sandy aluminium oxide through two-segment decomposition |
| CN106629798A (en) * | 2016-12-29 | 2017-05-10 | 东北大学设计研究院（有限公司） | Novel two-stage-decomposition intensive system and process for producing sandy aluminum oxide |
| CN106986362A (en) * | 2017-04-12 | 2017-07-28 | 柳健康 | A kind of sodium aluminate solution high concentration is low admittedly containing one section of seeded precipitation technique |
| CN111410221A (en) * | 2020-03-26 | 2020-07-14 | 重庆市南川区先锋氧化铝有限公司 | Be applicable to crystal seed processing apparatus among sodium aluminate production technology |
| CN111410221B (en) * | 2020-03-26 | 2022-11-08 | 重庆市九龙万博新材料科技有限公司 | Be applicable to crystal seed processing apparatus among sodium aluminate production technology |
| CN114264171A (en) * | 2021-12-09 | 2022-04-01 | 沈阳铝镁设计研究院有限公司 | Semen cooling device and process for two-stage decomposition |
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