CN103723742A - Post-treatment method for washing, drying and calcining SAPO (silicoaluminophosphate) molecular sieve - Google Patents
Post-treatment method for washing, drying and calcining SAPO (silicoaluminophosphate) molecular sieve Download PDFInfo
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Abstract
The invention discloses a post-treatment process for washing, drying and calcining an SAPO (silicoaluminophosphate) molecular sieve. The process is characterized in that aiming at the production characteristics of an SAPO molecular sieve, a crystalized molecular sieve stock solution is filtered by a primary section of a belt filter, and is washed twice by secondary and tertiary sections of the belt filter, and is formed into a filter cake at the tail end of the belt filter; the filter cake is dried by using a spin flash drying device to form dried fine powder; and the dried fine powder is collected by a cloth envelope collector, and is calcined by using a rotary kiln to complete removing an organic amine template agent in a molecular sieve channel, so that the SAPO molecular sieve product with catalytic activity can be obtained. Meanwhile, high-temperature tail gas generated in calcination of the rotary kiln can be used as a heat source and returned to the spin flash drying device. The process has the characteristics of continuous operation, high automatic degree, sufficient utilization of high-temperature heat source, low comprehensive energy consumption, and no dust pollution because dust is operated in closed equipment or pipeline.
Description
Technical field
The invention belongs to Chemical Manufacture Technology field, relate to particularly a kind of washing of SAPO molecular sieve, dry and roasting post-treating method.
Background technology
SAPO molecular sieve has good catalytic activity, especially at methanol-to-olefins technical field development field.The use of SAPO molecular sieve can realize methyl alcohol and replace oil to become the raw material of producing alkene, thereby depending on unduly oil broken away from the preparation of alkene.For the large area of some coal storages, possesses very important strategic importance.
In recent years, SAPO molecular sieve is the focus that catalyst field is paid close attention to always, possesses good application prospect.For synthetic SAPO molecular sieve treatment process document, there is report.General comparatively traditional method is as follows, uses flame filter press to carry out filtration washing several times to synthetic SAPO molecular sieve pulp, obtains filter cake; Then filter cake is put in saggar, by large baking oven, it is carried out to drying and processing, finally the SAPO molecular sieve after the oven dry obtaining is ground and puts into stoving oven and carry out roasting, after roasting, obtain having the SAPO molecular sieve of catalytic activity.But, in Plate Filtration operation process, have that consumption manpower, water loss are large, the problem of length consuming time, dry simultaneously and roasting process exist consume manpower, the problem such as large, the length consuming time of consuming energy.These problems affect the preparation process of SAPO molecular sieve greatly, and therefore, a kind of new SAPO molecular sieve treatment process is urgently developed and applied.
Summary of the invention
The present invention, for solving the problems of the technologies described above, provides a kind of washing of SAPO molecular sieve, dry and roasting post-treating method, and this technological operation is continuous, level of automation is high, and dust all operates in Sealing Arrangement or pipeline, no dust pollution, high temperature heat source makes full use of, and comprehensive energy consumption is low.The concrete technical scheme adopting is as follows:
The washing of SAPO molecular sieve, a dry and roasting post-treating method, comprise that step is as follows:
Step 1: the molecular sieve mother liquor of the form that adopts multistage band filter after to crystallization washs, and the SAPO molecular sieve after washing finally forms filter cake at the end of band filter;
Step 2: use Spin Flash Dryer to pulverize the molecular sieve after dry filter;
Step 3: use rotary kiln to carry out roasting to molecular sieve, the high-temperature tail gas that rotary kiln baking produces turns back to rotary flash distillation device as thermal source;
Step 4: the SAPO molecular sieve that obtains having catalytic activity through above treating processes.
The molecular sieve mother liquor of the form that described step 1 adopts three sections of band filters after to crystallization washs, and concrete washing step is as follows:
(1) the molecular sieve mother liquor after crystallization is carried out molecular sieve and mother liquor with a section of band filter separation, at the lower end of one section of band filter placing container, collect mother liquor;
(2) two sections at band filter are used distilled water to filter, and collect once washing liquid in the lower end of two sections of band filters simultaneously;
(3) at three sections of band filter, use de-salted waters to filter, in the lower end of three sections of band filters, collect secondary washing liquid simultaneously, and the secondary washing liquid of collection is led and got back to two sections of band filter for washing the molecular sieve on two sections of band filters.
Multi-stage type filter described in step 1, operation hop count is not less than three sections.The filter cloth lower end of multistage band filter is low pressure or vacuum state, to guarantee the carrying out of filtration washing process.
Described step 2 is used Spin Flash Dryer to the rapid grinding dispersion of block filter cake dry rapidly.The dried molecular sieve fine powder of Spin Flash Dryer will be collected through cloth envelop collector, then use rotary kiln to carry out roasting to fine powder, object is thoroughly to remove the organic amine template in molecular sieve pore passage, obtains having the SAPO zeolite product of catalytic activity.Spin Flash Dryer, the inlet temperature of rotary flash distillation is not less than 400 ℃, the mass ratio of hot blast and material and hot blast temperature (℃) product be not less than 1000, simultaneously in the filter cake of ingress, the mass content of water is not more than 50%.The dry fine powder particle diameter that Spin Flash Dryer filtration cakes torrefaction forms is less than 20 microns, and the water-content of dry fine powder is not more than 8% simultaneously.The mass ratio of described hot blast and material refers to the quality of the required warm air of Spin Flash Dryer inner drying certain mass material, and hot blast temperature is exactly the temperature in finger device, and under steady temperature, the quality of the drier material of the amount of hot blast is larger; In other words under the amount of identical hot blast, dry more materials be exactly need to be higher temperature.
Described in step 3, the high temperature section temperature of rotary kiln is controlled at 550 ℃-800 ℃, and molecular sieve is at the residence time of high temperature section 4-10h, the residence time 2-4h from rotary kiln entrance to high temperature section.
The invention has the beneficial effects as follows: the present invention operates continuously, and level of automation is high, dust all operates in Sealing Arrangement or pipeline, no dust pollution, and high temperature heat source makes full use of, and comprehensive energy consumption is low.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention
Marginal data: 1, one section of band filter, 2, two sections of band filters, 3, three sections of band filters, 4, Spin Flash Dryer, 5, cloth envelop collector, 6, rotary kiln
A, molecular sieve mother liquor, B, mother liquor, C, secondary washing liquid, D, once washing liquid, E, de-salted water, F, filter cake, G, molecular sieve fine powder, H, high-temperature tail gas, I, have the SAPO molecular sieve of catalytic activity
Embodiment
For technique means, creation characteristic that the present invention is realized, reach object and effect is easy to understand, below the specific embodiment of the present invention is described further, but does not limit protection scope of the present invention.
Embodiment 1:
The SAPO molecular sieve mother liquor A of 500Kg after crystallization is first filtered for one section 1 with band filter, isolate mother liquor B, then at two section 2 of band filter, band filter, carry out twice washing for three section 3, wherein three section of 3 use de-salted water E washing of band filter, the secondary washing liquid C obtaining is led and is back to band filter and washs for two section 2, filter out once washing liquid, reach the object of recycle, finally at the end of band filter, form filter cake F; Then use the dry molecular sieves fine powder G that Spin Flash Dryer 4 is 6-12 micron by the dry formation of filter cake F particle diameter at 400 ℃; Dry molecular sieves fine powder G is used rotary kiln 6 to carry out roasting to molecular sieve fine powder G after cloth envelop collector 5 is collected, maturing temperature is 550 ℃, roasting time 4h, the residence time from rotary kiln entrance to high temperature section is 2h, finally obtains having the SAPO molecular sieve I product 213Kg of catalytic activity.The high-temperature tail gas H that rotary kiln 6 roastings simultaneously produce turns back to Spin Flash Dryer 4 as thermal source.
Embodiment 2:
The SAPO molecular sieve mother liquor A of 1200Kg after crystallization is first filtered for one section 1 with band filter, isolate mother liquor B, then at two section 2 of band filter, band filter, carry out twice washing for three section 3, wherein three section of 3 use de-salted water E washing of band filter, the secondary washing liquid C obtaining is led and is back to band filter and washs for two section 2, filter out once washing liquid, reach the object of recycle, finally at the end of band filter, form filter cake F; Then use the dry molecular sieves fine powder G that Spin Flash Dryer 4 is 8-13 micron by the dry formation of filter cake F particle diameter at 600 ℃; Dry molecular sieves fine powder G is used rotary kiln 6 to carry out roasting to molecular sieve fine powder G after cloth envelop collector 5 is collected, maturing temperature is 700 ℃, roasting time 6h, the residence time from rotary kiln entrance to high temperature section is 3h, finally obtains having the SAPO molecular sieve I product 452Kg of catalytic activity.The high-temperature tail gas H that rotary kiln 6 roastings simultaneously produce turns back to Spin Flash Dryer 4 as thermal source.
Embodiment 3:
The SAPO molecular sieve mother liquor A of 800Kg after crystallization is first filtered for one section 1 with band filter, isolate mother liquor B, then at two section 2 of band filter, band filter, carry out twice washing for three section 3, wherein three section of 3 use de-salted water E washing of band filter, the secondary washing liquid C obtaining is led and is back to band filter and washs for two section 2, filter out once washing liquid, reach the object of recycle, finally at the end of band filter, form filter cake F; Then use the dry molecular sieves fine powder G that Spin Flash Dryer 4 is 2-16 micron by the dry formation of filter cake F particle diameter at 500 ℃; Dry molecular sieves fine powder G is used rotary kiln 6 to carry out roasting to molecular sieve fine powder G after cloth envelop collector 5 is collected, maturing temperature is 620 ℃, roasting time 5h, the residence time from rotary kiln entrance to high temperature section is 3h, finally obtains having the SAPO molecular sieve I product 307Kg of catalytic activity.The high-temperature tail gas H that rotary kiln 6 roastings simultaneously produce turns back to Spin Flash Dryer 4 as thermal source.
Embodiment 4:
The SAPO molecular sieve mother liquor A of 1500Kg after crystallization is first filtered for one section 1 with band filter, isolate mother liquor B, then at two section 2 of band filter, band filter, carry out twice washing for three section 3, wherein three section of 3 use de-salted water E washing of band filter, the secondary washing liquid C obtaining is led and is back to band filter and washs for two section 2, filter out once washing liquid, reach the object of recycle, finally at the end of band filter, form filter cake F; Then use the dry molecular sieves fine powder G that Spin Flash Dryer 4 is 4-9 micron by the dry formation of filter cake F particle diameter at 780 ℃; Dry molecular sieves fine powder G is used rotary kiln 6 to carry out roasting to molecular sieve fine powder G after cloth envelop collector 5 is collected, maturing temperature is 660 ℃, roasting time 9h, the residence time from rotary kiln entrance to high temperature section is 4h, finally obtains having the SAPO molecular sieve I product 622Kg of catalytic activity.The high-temperature tail gas H that rotary kiln 6 roastings simultaneously produce turns back to Spin Flash Dryer 4 as thermal source.
Processing method of the present invention is described by specific embodiment.Those skilled in the art can use for reference the links such as content appropriate change raw material of the present invention, processing condition and realize corresponding other object, its relevant change does not all depart from content of the present invention, within all similar replacements and change will become apparent to those skilled in the art that and be all deemed to be included in scope of the present invention.
Claims (9)
1. the washing of SAPO molecular sieve, a dry and roasting post-treating method, is characterized in that, comprises that step is as follows:
Step 1: the molecular sieve mother liquor of the form that adopts multistage band filter after to crystallization washs, and the SAPO molecular sieve after washing finally forms filter cake at the end of band filter;
Step 2: use Spin Flash Dryer to pulverize the molecular sieve after dry filter;
Step 3: use rotary kiln to carry out roasting to molecular sieve, the high-temperature tail gas that rotary kiln baking produces turns back to rotary flash distillation device as thermal source;
Step 4: the SAPO molecular sieve that obtains having catalytic activity through above treating processes.
2. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, is characterized in that, the molecular sieve mother liquor of the form that described step 1 adopts three sections of band filters after to crystallization washs, and specifically washing step is as follows:
(1) the molecular sieve mother liquor after crystallization is carried out molecular sieve and mother liquor with a section of band filter separation, at the lower end of one section of band filter placing container, collect mother liquor;
(2) two sections at band filter are used distilled water to filter, and collect once washing liquid in the lower end of two sections of band filters simultaneously;
(3) at three sections of band filter, use de-salted waters to filter, in the lower end of three sections of band filters, collect secondary washing liquid simultaneously, and the secondary washing liquid of collection is led and got back to two sections of band filter for washing the molecular sieve on two sections of band filters.
3. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, is characterized in that, multi-stage type filter described in step 1, operates hop count and be not less than three sections.
4. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, is characterized in that, the filter cloth lower end of multistage band filter is low pressure or vacuum state described in step 1.
5. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, is characterized in that, described step 2 is used Spin Flash Dryer to the rapid grinding dispersion of block filter cake dry rapidly.
6. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, it is characterized in that, described in step 2, the dried molecular sieve fine powder of Spin Flash Dryer will be collected through cloth envelop collector, then uses rotary kiln to carry out roasting to fine powder.
7. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, it is characterized in that, Spin Flash Dryer described in step 2, the inlet temperature of rotary flash distillation is not less than 400 ℃, the mass ratio of hot blast and material and hot blast temperature (℃) product be not less than 1000, simultaneously in the filter cake of ingress, the mass content of water is not more than 50%.
8. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, it is characterized in that, Spin Flash Dryer described in step 2, the dry fine powder particle diameter that filtration cakes torrefaction forms is less than 20 microns, and the water-content of dry fine powder is not more than 18% simultaneously.
9. a kind of washing of SAPO molecular sieve according to claim 1, dry and roasting post-treating method, it is characterized in that, described in step 3, the high temperature section temperature of rotary kiln is controlled at 550 ℃-800 ℃, molecular sieve is at the residence time of high temperature section 4-10h, the residence time 2-4h from rotary kiln entrance to high temperature section.
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103979569A (en) * | 2014-06-04 | 2014-08-13 | 陕西省煤化工工程技术研究中心 | Preparation method of silicoaluminophosphate molecular sieve with hierarchical pore structure |
| CN105651031A (en) * | 2014-12-06 | 2016-06-08 | 中国石油化工股份有限公司 | Spin flash drying equipment and spin flash drying method |
| CN106430228A (en) * | 2016-09-08 | 2017-02-22 | 中国石油化工股份有限公司 | Molecular sieve crystallization mother liquor treatment method |
| CN106672989A (en) * | 2017-03-27 | 2017-05-17 | 上海恒业分子筛股份有限公司 | Production equipment of molecular sieve activated powder and method for producing molecular sieve activated powder |
| CN106830009A (en) * | 2017-01-25 | 2017-06-13 | 中国天辰工程有限公司 | A kind of method of reuse sial phosphorus molecular sieve filtered fluid and molecular sieve device is prepared again |
| CN107021509A (en) * | 2017-05-12 | 2017-08-08 | 中国天辰工程有限公司 | A kind of drying and roasting of sial phosphorus molecular sieve fine powder and the method reclaimed |
| CN107176614A (en) * | 2017-05-16 | 2017-09-19 | 中国天辰工程有限公司 | A kind for the treatment of fluid for washing sial phosphorus molecular sieve and the method for detecting amine component and content in the treatment fluid |
| CN114477218A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Molecular sieve crystallization slurry cleaning equipment and cleaning method |
| CN114516644A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Drying and crushing method of SAPO-34 molecular sieve |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101264900A (en) * | 2008-05-05 | 2008-09-17 | 洛阳市建龙化工有限公司 | Method for preparing large-grain 4A-type molecular screen primary powder |
| CN101428819A (en) * | 2007-11-09 | 2009-05-13 | 汉能科技有限公司 | Process for producing SAPO-5 molecular sieve |
| CN101654257A (en) * | 2009-10-21 | 2010-02-24 | 中国铝业股份有限公司 | Method for preparing 4A zeolite by continuous crystallization |
| CN202829600U (en) * | 2012-08-31 | 2013-03-27 | 中国石油化工股份有限公司 | Continuous type rotary roasting furnace |
-
2013
- 2013-12-31 CN CN201310756440.5A patent/CN103723742A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101428819A (en) * | 2007-11-09 | 2009-05-13 | 汉能科技有限公司 | Process for producing SAPO-5 molecular sieve |
| CN101264900A (en) * | 2008-05-05 | 2008-09-17 | 洛阳市建龙化工有限公司 | Method for preparing large-grain 4A-type molecular screen primary powder |
| CN101654257A (en) * | 2009-10-21 | 2010-02-24 | 中国铝业股份有限公司 | Method for preparing 4A zeolite by continuous crystallization |
| CN202829600U (en) * | 2012-08-31 | 2013-03-27 | 中国石油化工股份有限公司 | Continuous type rotary roasting furnace |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103979569A (en) * | 2014-06-04 | 2014-08-13 | 陕西省煤化工工程技术研究中心 | Preparation method of silicoaluminophosphate molecular sieve with hierarchical pore structure |
| CN105651031A (en) * | 2014-12-06 | 2016-06-08 | 中国石油化工股份有限公司 | Spin flash drying equipment and spin flash drying method |
| CN105651031B (en) * | 2014-12-06 | 2019-05-21 | 中国石油化工股份有限公司 | A kind of rotary flashing drying equipment and rotary flashing drying method |
| CN106430228B (en) * | 2016-09-08 | 2018-09-21 | 中国石油化工股份有限公司 | Molecular sieve mother solution processing method |
| CN106430228A (en) * | 2016-09-08 | 2017-02-22 | 中国石油化工股份有限公司 | Molecular sieve crystallization mother liquor treatment method |
| CN106830009A (en) * | 2017-01-25 | 2017-06-13 | 中国天辰工程有限公司 | A kind of method of reuse sial phosphorus molecular sieve filtered fluid and molecular sieve device is prepared again |
| CN106672989B (en) * | 2017-03-27 | 2019-02-26 | 上海恒业分子筛股份有限公司 | The production equipment of molecular sieve activation powder and the method for producing molecular sieve activation powder |
| CN106672989A (en) * | 2017-03-27 | 2017-05-17 | 上海恒业分子筛股份有限公司 | Production equipment of molecular sieve activated powder and method for producing molecular sieve activated powder |
| CN107021509B (en) * | 2017-05-12 | 2019-02-22 | 中国天辰工程有限公司 | A kind of method of the drying and roasting and recycling of sial phosphorus molecular sieve fine powder |
| CN107021509A (en) * | 2017-05-12 | 2017-08-08 | 中国天辰工程有限公司 | A kind of drying and roasting of sial phosphorus molecular sieve fine powder and the method reclaimed |
| CN107176614A (en) * | 2017-05-16 | 2017-09-19 | 中国天辰工程有限公司 | A kind for the treatment of fluid for washing sial phosphorus molecular sieve and the method for detecting amine component and content in the treatment fluid |
| CN114477218A (en) * | 2020-10-28 | 2022-05-13 | 中国石油化工股份有限公司 | Molecular sieve crystallization slurry cleaning equipment and cleaning method |
| CN114516644A (en) * | 2020-11-19 | 2022-05-20 | 中国石油化工股份有限公司 | Drying and crushing method of SAPO-34 molecular sieve |
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Application publication date: 20140416 |