CN115704647A - Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method - Google Patents
Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method Download PDFInfo
- Publication number
- CN115704647A CN115704647A CN202110913059.XA CN202110913059A CN115704647A CN 115704647 A CN115704647 A CN 115704647A CN 202110913059 A CN202110913059 A CN 202110913059A CN 115704647 A CN115704647 A CN 115704647A
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- drying
- unit
- supercritical
- treatment
- 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
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J13/00—Colloid chemistry, e.g. the production of colloidal materials or their solutions, not otherwise provided for; Making microcapsules or microballoons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B21/00—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects
- F26B21/14—Arrangements or duct systems, e.g. in combination with pallet boxes, for supplying and controlling air or gases for drying solid materials or objects using gases or vapours other than air or steam, e.g. inert gases
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B25/00—Details of general application not covered by group F26B21/00 or F26B23/00
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F26—DRYING
- F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
- F26B9/00—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards
- F26B9/06—Machines or apparatus for drying solid materials or objects at rest or with only local agitation; Domestic airing cupboards in stationary drums or chambers
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Abstract
The invention relates to the field of supercritical drying, and discloses a supercritical carbon dioxide drying device, application thereof and a supercritical carbon dioxide drying method, wherein the device comprises a supercritical processing unit, a drying unit and a separation unit which are sequentially communicated through pipelines, and the drying unit contains 3-12 drying kettles which are arranged in parallel; the supercritical processing unit is used for performing supercritical processing on the condensed carbon dioxide to obtain processed carbon dioxide; the drying unit is used for contacting the treated carbon dioxide with a material to be dried to carry out drying treatment, so as to obtain an effluent I; the separation unit is used for separating the effluent I to obtain carbon dioxide capable of being recycled and an effluent II. The supercritical carbon dioxide drying device and the supercritical carbon dioxide drying method provided by the invention have higher drying efficiency and lower energy consumption.
Description
Technical Field
The invention relates to the field of supercritical drying, in particular to a supercritical carbon dioxide drying device, application of the supercritical carbon dioxide drying device in preparation of aerogel and a supercritical carbon dioxide drying method.
Background
At present, carbon dioxide in the traditional supercritical carbon dioxide drying process generally adopts the feeding mode of going in and going out from the bottom, and carbon dioxide flows in from the bottom of drying kettle, and the top flows out, because the gravity influence of liquid substance in the material to be dried, carbon dioxide can not take the liquid substance out of the drying kettle completely, can only solve aforementioned problem through increasing the extraction time to lead to the reduction of work efficiency, cause the increase of energy consumption.
As is known, the solubility of the supercritical carbon dioxide at a certain pressure and temperature to the solute is certain, while the prior art drying kettles usually adopt a series connection mode, and since the solute cannot be completely carried out by the carbon dioxide, the carbon dioxide entering the next drying kettle inevitably contains a certain amount of solute, so that the amount of solute dissolved in the carbon dioxide in the next drying kettle is reduced. The larger the number of drying kettles, the more the amount of solute dissolved in carbon dioxide gradually decreases, resulting in the product quality of the latter drying kettle being inferior to that of the former drying kettle. The current solution to this phenomenon is to increase the extraction time to ensure the yield of the product, but this undoubtedly results in a reduction in efficiency and an increase in cost.
Meanwhile, the flow rate of carbon dioxide in the traditional supercritical carbon dioxide drying process is usually kept constant, however, experiments prove that in the initial drying stage, as the material to be dried contains more liquid substances, more liquid substances can be taken out by carbon dioxide introduced in the initial stage; however, the liquid material has decreased considerably during the later stages of drying, at which point it has lost its meaning to maintain a constant flow of carbon dioxide. This is clearly wasteful, resulting in an increase in energy consumption.
Disclosure of Invention
The invention aims to solve the problems of low drying efficiency and high energy consumption in the prior art.
In order to achieve the above object, a first aspect of the present invention provides a supercritical carbon dioxide drying apparatus comprising:
the device comprises a supercritical processing unit, a drying unit and a separation unit which are sequentially communicated through pipelines, wherein the drying unit comprises 3-12 drying kettles which are arranged in parallel;
the supercritical processing unit is used for performing supercritical processing on the condensed carbon dioxide to obtain processed carbon dioxide;
the drying unit is used for contacting the treated carbon dioxide with a material to be dried to carry out drying treatment, so as to obtain an effluent I;
the separation unit is used for separating the effluent I to obtain carbon dioxide capable of being recycled and an effluent II;
the arrangement of the pipelines in the drying unit enables the treated carbon dioxide to be introduced from the upper part of each drying kettle and to be led out from the lower part of each drying kettle.
A second aspect of the present invention provides the use of the supercritical carbon dioxide drying apparatus described in the first aspect above in the preparation of aerogels.
A third aspect of the present invention provides a supercritical carbon dioxide drying method which is performed in the supercritical carbon dioxide drying apparatus described in the foregoing first aspect, comprising:
(1) Introducing the condensed carbon dioxide into a supercritical treatment unit for supercritical treatment to obtain treated carbon dioxide;
(2) Introducing the treated carbon dioxide into drying kettles which are arranged in parallel in a drying unit to contact with a material to be dried so as to carry out drying treatment, thereby obtaining an effluent I;
(3) Introducing the effluent I into a separation unit for separation to obtain carbon dioxide capable of being recycled and an effluent II.
The supercritical carbon dioxide drying device provided by the invention has the following beneficial effects:
(1) The supercritical carbon dioxide drying device provided by the invention adopts a feeding mode of feeding from top to bottom, and can change the gravity of the solute into power from resistance.
(2) The drying kettles in the supercritical carbon dioxide drying device provided by the invention adopt a parallel connection mode, so that each drying kettle works independently, the problem that the content of solute in carbon dioxide is reduced along with the increase of the number of the drying kettles can be effectively solved, and the drying efficiency is improved.
(3) The supercritical carbon dioxide drying device provided by the invention can gradually reduce the flow of carbon dioxide by adopting a stepped carbon dioxide flow introduction mode, thereby reducing the energy consumption.
(4) The supercritical carbon dioxide drying device provided by the invention has the advantage of adjustable production scale, and can be adjusted according to actual production conditions.
Drawings
Fig. 1 is a diagram of a supercritical carbon dioxide drying apparatus according to a preferred embodiment of the present invention.
Description of the reference numerals
Y1-storage unit E1-condensing unit IP 1-booster pump E2-heat exchanger I
R1-drying kettle R2-drying kettle R3-drying kettle
E3-heat exchanger IIS 1-separation kettle E4-heat exchanger IIS 2-separation kettle
Y2-recovery Unit IY 3-recovery Unit IIC 1 compression Pump E5-condensation Unit II
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For numerical ranges, each range between its endpoints and individual point values, and each individual point value can be combined with each other to give one or more new numerical ranges, and such numerical ranges should be construed as specifically disclosed herein.
As previously described, a first aspect of the present invention provides a supercritical carbon dioxide drying apparatus comprising:
the device comprises a supercritical processing unit, a drying unit and a separation unit which are sequentially communicated through pipelines, wherein the drying unit comprises 3-12 drying kettles which are arranged in parallel;
the supercritical processing unit is used for performing supercritical processing on the condensed carbon dioxide to obtain processed carbon dioxide;
the drying unit is used for contacting the treated carbon dioxide with a material to be dried to carry out drying treatment, so as to obtain an effluent I;
the separation unit is used for separating the effluent I to obtain carbon dioxide capable of being recycled and an effluent II;
the arrangement of the lines in the drying unit enables the treated carbon dioxide to be introduced from the upper part of each drying vessel and to be withdrawn from the lower part of each drying vessel.
The inventor of the invention finds that compared with the prior art, the drying device provided by the invention has higher drying efficiency and lower energy consumption.
Preferably, the number of the drying kettles arranged in parallel in the drying unit is 3.
Preferably, the supercritical processing unit comprises a booster pump and a heat exchanger I which are communicated in sequence. It should be noted that the present invention has no particular limitation on the number of the booster pumps and the heat exchangers I, and those skilled in the art can select the number in combination with the techniques known in the art, and the present invention will not be described in detail herein, and those skilled in the art should not be construed as limiting the present invention. The invention exemplarily provides a preferable embodiment, in order to realize higher drying efficiency and lower energy consumption, the number of the booster pumps and the heat exchangers I in the invention is respectively 1, and a series connection mode that the booster pumps are arranged in front and the heat exchangers I are arranged in back is adopted.
Preferably, the separation unit comprises a heat exchanger II and a separation kettle which are sequentially communicated, and the heat exchanger II is communicated with the drying kettle.
Further preferably, the number of the heat exchangers II is at least 2, and the number of the separation kettles is at least 2. In the invention, the connection mode of the 2 heat exchangers II and the 2 separation kettles can be the heat exchanger II, and the separation kettle, the heat exchanger II and the separation kettle are sequentially connected in series, wherein the heat exchanger II is communicated with the drying kettle.
Preferably, the device further comprises a recovery unit I and a recovery unit II, the recovery unit I is arranged at the downstream of the separation unit and is communicated with the separation kettle, the recovery unit II is arranged at the downstream of the drying unit in parallel with the separation unit, the recovery unit I is used for recovering the effluent II, and the recovery unit II is used for recovering a part of the carbon dioxide capable of being recycled.
Preferably, the apparatus further comprises a storage unit disposed upstream of the supercritical processing unit, the storage unit being capable of storing carbon dioxide.
According to a preferred embodiment, the apparatus further comprises a condensation unit I arranged between the storage unit and the supercritical processing unit, for condensing the carbon dioxide withdrawn from the storage unit.
According to another preferred embodiment, the apparatus further comprises a condensing unit II disposed between the storage unit and the recovery unit II, the condensing unit II is configured to condense the remaining part of the recyclable carbon dioxide, and the raw material condensed by the condensing unit II is recycled to the storage unit.
It should be noted that the present invention has no particular limitation on the types of the drying kettle, the separation kettle and the heat exchanger, and those skilled in the art can select them in combination with the techniques known in the art, and the present invention will not be described in detail herein, and those skilled in the art should not be construed as limiting the present invention.
It should be noted that the present invention has no particular limitation on the type and number of the devices used in the storage unit, the condensation unit and the recovery unit, and those skilled in the art can select the devices in combination with the techniques known in the art, and the present invention will not be described in detail herein, and those skilled in the art should not be construed as limiting the present invention.
It is noted that various control valves known to those skilled in the art may be provided in the circulation path in the apparatus of the present invention to control the flow of the carbon dioxide fluid.
It should be noted that all pressure vessels (such as storage unit, drying kettle, separation kettle, heat exchanger, condensing unit) in the apparatus of the present invention may have independent evacuation valves, and may also have pressure gauges and temperature gauges to display the pressure and temperature in the apparatus. The carbon dioxide storage unit and the carbon dioxide recovery unit can also be provided with a carbon dioxide volume meter to display the volume of liquid carbon dioxide in the device. Each drying vessel may be provided with a flow meter to indicate the flow of carbon dioxide introduced into each drying vessel. In order to implement a cyclic process, the individual devices of the device according to the invention can be arranged or configured to match one another according to specific requirements.
It should be noted that the separation tank of the apparatus of the present invention may be filled with a material capable of adsorbing a solvent (solvent in the material to be dried), including but not limited to molecular sieve, and the material may be replaced and activated periodically.
The supercritical carbon dioxide drying apparatus according to the present invention will be described below with reference to fig. 1.
Leading a carbon dioxide raw material from a storage unit Y1 to a condensation unit I E1 for condensation treatment I, leading the condensed carbon dioxide to a pressure pump P1 for pressure treatment, leading the carbon dioxide subjected to pressure treatment to a heat exchanger I E2 for heating treatment to obtain carbon dioxide in a supercritical state, leading the carbon dioxide in the supercritical state to a drying kettle R1, a drying kettle R2 and a drying kettle R3 respectively for drying treatment (simultaneously or singly), leading the carbon dioxide carrying a solvent to a heat exchanger II E3 and/or a heat exchanger II E4 for heating treatment after the drying treatment, leading the carbon dioxide into a separation kettle S1 and/or a separation kettle S2 for separation after the heating treatment, leading an effluent II obtained by separation into a recovery unit I Y2 for recovery treatment, leading part of the carbon dioxide capable of being recycled to a recovery unit IIY3, leading the rest part of the carbon dioxide into a condensation unit II E5 for condensation treatment II after the compression treatment by a compression pump C1, and circularly using the carbon dioxide in the storage unit II subjected to condensation treatment II for recycling. The carbon dioxide in the recovery unit IIY3 can be compressed by the compression pump C1 when the device is not in operation and then introduced into the condensation unit II E5 for condensation treatment II, and the carbon dioxide after condensation treatment II is introduced into the storage unit Y1 for recycling.
As previously mentioned, a second aspect of the present invention provides the use of the supercritical carbon dioxide drying apparatus described in the first aspect above in the preparation of aerogels.
As described above, the third aspect of the present invention provides a supercritical carbon dioxide drying method which is performed in the supercritical carbon dioxide drying apparatus described in the foregoing first aspect, comprising:
(1) Introducing the condensed carbon dioxide into a supercritical treatment unit for supercritical treatment to obtain treated carbon dioxide;
(2) Introducing the treated carbon dioxide into drying kettles arranged in parallel in a drying unit to contact with a material to be dried so as to carry out drying treatment, thereby obtaining an effluent I;
(3) Introducing the effluent I into a separation unit for separation to obtain carbon dioxide capable of being recycled and an effluent II.
Preferably, the method further comprises, before step (1), introducing the carbon dioxide raw material in the storage unit into a condensation unit I for condensation treatment I to obtain the condensed carbon dioxide. The purpose of the condensation treatment I is to prevent carbon dioxide from vaporizing, thereby ensuring that the pressure pump can deliver carbon dioxide to each of the drying kettles.
According to a preferred embodiment, the method further comprises, after carrying out said step (3), introducing said effluent II into a recovery unit I for recovery treatment, introducing a portion of said recyclable carbon dioxide into a recovery unit II and recycling the remaining portion of said recyclable carbon dioxide into a condensation unit II for condensation treatment II, and introducing the material obtained after carrying out said condensation treatment II into said storage unit.
Preferably, the volume ratio of the part of the recyclable carbon dioxide to the remaining part of the recyclable carbon dioxide is 1:0.83-0.95. The inventor of the invention finds that in the preferable condition, the drying method provided by the invention has lower energy consumption.
According to another preferred embodiment, in the step (2), the conditions of the drying treatment in each of the drying tanks are the same or different, and each independently at least: controlling the flow rate of the treated carbon dioxide to be 800-1500L/h.
In order to achieve higher drying efficiency and lower energy consumption, it is preferable that the drying conditions in each drying kettle independently at least satisfy:
when the drying treatment is carried out for 0-2h, controlling the flow rate of the treated carbon dioxide to be 1200-1500L/h;
when the drying treatment is carried out for 2-4h, controlling the flow of the treated carbon dioxide to be 1000-1200L/h;
and when the drying treatment is carried out for 4-6h, controlling the flow of the treated carbon dioxide to be 800-1000L/h.
In the apparatus of the present invention, the pressure and temperature of the apparatuses in the storage unit, the drying unit, and the separation unit are not particularly limited. Illustratively, the pressure in the storage unit means may be from 4 to 5MPa, the temperature from 7 to 15 ℃, the pressure in the drying unit means may be from 13 to 16MPa, the temperature from 50 to 70 ℃, the pressure in the separation unit means may be from 4 to 8MPa, and the temperature from 40 to 60 ℃.
It should be noted that all timing starts in the present invention are when the inlet valve of the drying kettle is opened to start introducing the treated carbon dioxide. And when the drying treatment is carried out for 0-2h, the step of opening an inlet valve of the drying kettle to start introducing the treated carbon dioxide is carried out for 2h. Similarly, when the drying treatment is carried out for 2 to 4 hours, the treated carbon dioxide is introduced for 2 hours to 4 hours. Those skilled in the art can do so, and the detailed description of the present invention is omitted here.
The drying treatment in the invention is preferably a batch drying treatment, namely, the inlet valve of the drying kettle is temporarily closed after the product is dried, so as to carry out the loading and unloading treatment of the product.
The present invention will be described in detail below by way of examples.
In the following examples, the preparation of the wet gel to be dried is carried out: the wet gel to be dried was prepared according to the method in example 1 in CN 103118979A.
A carbon dioxide storage tank: the volume is 10m 3 。
A carbon dioxide drying kettle: a volume of 3m 3 。
A separation kettle: volume of 3m 3 。
A solvent recovery tank: a volume of 1m 3 。
A carbon dioxide recovery tank: a volume of 3m 3 。
Example 1
The method comprises the steps of placing 750L of wet gel to be dried into each drying kettle, introducing carbon dioxide subjected to condensation treatment into each drying kettle, carrying out drying treatment, after drying treatment is finished, cooling and depressurizing an effluent I, introducing the effluent I into a separation kettle for separation treatment, when the liquid level of a solvent in a solvent recovery tank reaches a set liquid level (4/5 of the volume of equipment), carrying out solvent recovery treatment, after separation treatment is finished, firstly carrying out pressure balance on the drying kettle and a carbon dioxide storage tank, compressing and condensing a part of carbon dioxide, then circulating the carbon dioxide to the carbon dioxide storage tank, then carrying out pressure balance on the carbon dioxide recovery tank, and introducing the rest of carbon dioxide into the carbon dioxide recovery tank, wherein the carbon dioxide in the carbon dioxide recovery tank can be compressed and condensed and introduced into the carbon dioxide storage tank when the equipment does not operate. And calculating the drying efficiency and energy consumption. The condition parameters of each apparatus and the parameters of the drying process are shown in Table 1, and the results of the drying efficiency and energy consumption are shown in Table 2.
Examples 2 to 6
Examples 2-6 were carried out in a similar manner to the examples, except that the conditions in the apparatus and the drying process were as specified in Table 1, and the results are as shown in Table 2.
Comparative example 1
This comparative example was carried out in a similar manner to example 1, except that: the arrangement of the pipelines was adjusted so that the treated carbon dioxide was introduced from the lower part of the drying kettle and was introduced from the upper part of the drying kettle, and the specific drying conditions and results are shown in Table 1 and Table 2, respectively.
Comparative example 2
This comparative example was carried out in a similar manner to example 1, except that: and adjusting the connection mode of the drying kettles to ensure that the drying kettles are communicated in a series connection mode, and the carbon dioxide entering the next drying kettle is led out from the previous drying kettle, wherein the specific drying conditions are shown in a table 1, and the results are shown in a table 2.
Comparative example 3
This comparative example was carried out in a similar manner to example 1, except that: the connection mode of the drying kettles is adjusted, so that the drying kettles are communicated in a series connection mode, carbon dioxide entering the next drying kettle is led out from the previous drying kettle, and the arrangement of pipelines is adjusted, so that the treated carbon dioxide is led in from the lower part of the drying kettle and led out from the upper part of the drying kettle, the specific drying conditions are shown in table 1, and the results are shown in table 2.
Drying efficiency: the weight of the recovered solvent per unit time in kg/h.
TABLE 1
TABLE 1
TABLE 2
As can be seen from the results in table 2, the supercritical carbon dioxide drying apparatus and the supercritical carbon dioxide drying method provided by the present invention have high drying efficiency and low energy consumption.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (10)
1. A supercritical carbon dioxide drying apparatus, characterized in that the apparatus comprises:
the device comprises a supercritical processing unit, a drying unit and a separation unit which are sequentially communicated through pipelines, wherein the drying unit comprises 3-12 drying kettles which are arranged in parallel;
the supercritical processing unit is used for performing supercritical processing on the condensed carbon dioxide to obtain processed carbon dioxide;
the drying unit is used for contacting the treated carbon dioxide with a material to be dried to carry out drying treatment, so as to obtain an effluent I;
the separation unit is used for separating the effluent I to obtain carbon dioxide capable of being recycled and an effluent II;
the arrangement of the lines in the drying unit enables the treated carbon dioxide to be introduced from the upper part of each drying vessel and to be withdrawn from the lower part of each drying vessel.
2. The device of claim 1, wherein the number of drying kettles arranged in parallel in the drying unit is 3;
preferably, the supercritical processing unit comprises a booster pump and a heat exchanger I which are communicated in sequence;
preferably, the separation unit comprises a heat exchanger II and a separation kettle which are sequentially communicated, and the heat exchanger II is communicated with the drying kettle;
preferably, the number of the heat exchangers II is at least 2, and the number of the separation kettles is at least 2.
3. The apparatus according to claim 2, wherein the apparatus further comprises a recovery unit I and a recovery unit II, the recovery unit I is arranged at the downstream of the separation unit and communicated with the separation kettle, the recovery unit II is arranged at the downstream of the drying unit in parallel with the separation unit, the recovery unit I is used for recovering the effluent II, and the recovery unit II is used for recovering a part of the carbon dioxide which can be recycled.
4. The apparatus of any one of claims 1-3, wherein the apparatus further comprises a storage unit disposed upstream of the supercritical processing unit, the storage unit capable of storing carbon dioxide.
5. The apparatus according to claim 4, wherein the apparatus further comprises a condensing unit I disposed between the storage unit and the supercritical processing unit, the condensing unit I being configured to condense the carbon dioxide drawn out of the storage unit;
preferably, the device further comprises a condensation unit II arranged between the storage unit and the recovery unit II, and the condensation unit II is used for condensing the rest part of the carbon dioxide which can be recycled.
6. Use of the supercritical carbon dioxide drying apparatus of any one of claims 1 to 5 in the preparation of aerogels.
7. A supercritical carbon dioxide drying method which is carried out in the supercritical carbon dioxide drying apparatus according to any one of claims 1 to 5, comprising:
(1) Introducing the condensed carbon dioxide into a supercritical treatment unit for supercritical treatment to obtain treated carbon dioxide;
(2) Introducing the treated carbon dioxide into drying kettles which are arranged in parallel in a drying unit to contact with a material to be dried so as to carry out drying treatment, thereby obtaining an effluent I;
(3) Introducing the effluent I into a separation unit for separation to obtain carbon dioxide capable of being recycled and an effluent II.
8. The method of claim 7, further comprising, before said step (1), introducing the carbon dioxide raw material in the storage unit into a condensation unit I to perform condensation treatment I to obtain the condensed carbon dioxide;
preferably, the method further comprises, after performing the step (3), introducing the effluent II into a recovery unit I for recovery treatment, introducing a part of the recyclable carbon dioxide into the recovery unit II, and recycling the remaining part of the recyclable carbon dioxide into a condensation unit II for condensation treatment II, and introducing the material obtained after performing the condensation treatment II into the storage unit.
9. The method according to claim 7 or 8, wherein in step (2), the conditions of the drying treatment in each of the drying tanks are the same or different, each independently satisfying at least: controlling the flow rate of the treated carbon dioxide to be 800-1500L/h.
10. The method of claim 9, wherein the conditions of the drying process in each of the drying vessels each independently at least satisfy:
when the drying treatment is carried out for 0-2h, controlling the flow rate of the treated carbon dioxide to be 1200-1500L/h;
when the drying treatment is carried out for 2-4h, controlling the flow of the treated carbon dioxide to be 1000-1200L/h;
and when the drying treatment is carried out for 4-6h, controlling the flow of the treated carbon dioxide to be 800-1000L/h.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110913059.XA CN115704647A (en) | 2021-08-10 | 2021-08-10 | Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method |
| PCT/CN2022/107779 WO2023016240A1 (en) | 2021-08-10 | 2022-07-26 | Supercritical carbon dioxide drying apparatus and application thereof, and supercritical carbon dioxide drying method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110913059.XA CN115704647A (en) | 2021-08-10 | 2021-08-10 | Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115704647A true CN115704647A (en) | 2023-02-17 |
Family
ID=85179466
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202110913059.XA Pending CN115704647A (en) | 2021-08-10 | 2021-08-10 | Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN115704647A (en) |
| WO (1) | WO2023016240A1 (en) |
Family Cites Families (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103130454B (en) * | 2011-11-29 | 2014-12-24 | 航天特种材料及工艺技术研究所 | Low heat conductance silicon rubber foam material and manufacture method thereof |
| CN102491326B (en) * | 2011-11-30 | 2014-06-25 | 航天特种材料及工艺技术研究所 | Device for drying supercritical fluid and method for preparing aerogel material |
| CN103435320B (en) * | 2013-08-19 | 2016-05-04 | 航天特种材料及工艺技术研究所 | A kind of high-performance aerogel composite and preparation method thereof and equipment |
| CN107140939B (en) * | 2017-05-16 | 2019-07-12 | 纳诺科技有限公司 | A kind of production technology and process units of fiber composite aerogel blanket |
| CN108636304B (en) * | 2018-05-16 | 2021-04-30 | 航天特种材料及工艺技术研究所 | Method for preparing aerogel by supercritical drying method and device for supercritical drying |
| CN208205734U (en) * | 2018-05-17 | 2018-12-07 | 湖北远固新型建材科技股份有限公司 | A kind of ardealite tray drying kettle |
| CN108955096B (en) * | 2018-05-22 | 2020-04-17 | 航天特种材料及工艺技术研究所 | Supercritical carbon dioxide drying method |
| CN112672819A (en) * | 2018-09-12 | 2021-04-16 | 巴斯夫欧洲公司 | Method for continuous supercritical drying of aerogel particles |
| KR102429099B1 (en) * | 2018-12-20 | 2022-08-04 | 주식회사 엘지화학 | Supercritical drying method for silica wetgel blanket |
| CN111111572B (en) * | 2020-01-21 | 2023-10-20 | 中化学华陆新材料有限公司 | Supercritical CO in silicon-based aerogel production 2 Method for recovering dry solvent |
| CN113108558A (en) * | 2021-05-14 | 2021-07-13 | 中昊光明化工研究设计院有限公司 | Supercritical carbon dioxide drying device and drying method thereof |
-
2021
- 2021-08-10 CN CN202110913059.XA patent/CN115704647A/en active Pending
-
2022
- 2022-07-26 WO PCT/CN2022/107779 patent/WO2023016240A1/en active Search and Examination
Also Published As
| Publication number | Publication date |
|---|---|
| WO2023016240A1 (en) | 2023-02-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US8673112B2 (en) | Method and device for thermal hydrolysis and steam explosion of biomass | |
| CN102240464B (en) | Method for dynamic extraction by utilizing subcritical fluid | |
| US8366887B2 (en) | Hydrogen generating system and operating method therefor | |
| WO2022055809A1 (en) | Carbon dioxide extraction processes, devices, methods, and systems | |
| CN115704647A (en) | Supercritical carbon dioxide drying device and application thereof, and supercritical carbon dioxide drying method | |
| US20130092522A1 (en) | Pure Liquid Manufacturing Apparatus | |
| CN109000217B (en) | Full-circulation system and method for feeding water and adding ammonia of power plant boiler | |
| CN104803538B (en) | A kind of low cost, low energy consumption process the process of sea water | |
| JP2012241719A (en) | Method and apparatus for compressing gaseous medium in single or multiple stages | |
| CN201823337U (en) | Concentrating and crystallizing equipment for 5-hydroxyl tryptophan | |
| CN206027122U (en) | Multistage multi -chambered evaporimeter | |
| CN107512811A (en) | The processing method of ball-shape nickel hydroxide production process waste water | |
| CN108211801A (en) | A kind of multiple-effect distillation device, system and method | |
| CN210855897U (en) | For high content of CO2Ethane gas deep purification device | |
| CN207871568U (en) | A kind of gynostemma pentaphyllum extracting solution high-efficiency scraper enrichment facility | |
| CN207581358U (en) | One kind contains SO3Gas relieving haperacidity energy recycle device | |
| CN106753631A (en) | The process of reinforcing desorption type methane purification and recovery carbon dioxide | |
| US10220371B2 (en) | Molecular sieve depressurization system utilizing a low pressure inductor type vapor condenser | |
| RU2435458C1 (en) | Method for production of natural water and concentrated juice | |
| CN204853436U (en) | LNG waste boiler steam pocket feedwater deoxidization system | |
| CN109160622A (en) | One primary yeast evaporation condensate processing method and its dedicated unit | |
| CN115634677B (en) | Activated carbon desorption method and activated carbon desorption equipment | |
| CN201249046Y (en) | Multistage flash evaporator | |
| RU2326053C2 (en) | Method and device for evaporation of uranium hexafluoride from conatiners | |
| RU2435457C1 (en) | Device for production of natural water and concentrated juice |
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 |