WO2010024643A1 - Ethanol dehydration device of multi-tube type using pressure swing adsorption process - Google Patents

Ethanol dehydration device of multi-tube type using pressure swing adsorption process Download PDF

Info

Publication number
WO2010024643A1
WO2010024643A1 PCT/KR2009/004886 KR2009004886W WO2010024643A1 WO 2010024643 A1 WO2010024643 A1 WO 2010024643A1 KR 2009004886 W KR2009004886 W KR 2009004886W WO 2010024643 A1 WO2010024643 A1 WO 2010024643A1
Authority
WO
WIPO (PCT)
Prior art keywords
ethanol
tube
absorbent
dehydration device
dehydrated
Prior art date
Application number
PCT/KR2009/004886
Other languages
French (fr)
Inventor
Gi-Wook Choi
Byung-Wook Jang
Jun-Seong Jeong
Kyoung-Mo Go
Original Assignee
Changhae Ethanol Co., Ltd.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Changhae Ethanol Co., Ltd. filed Critical Changhae Ethanol Co., Ltd.
Publication of WO2010024643A1 publication Critical patent/WO2010024643A1/en

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/261—Drying gases or vapours by adsorption
    • 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
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
    • B01J20/16—Alumino-silicates
    • B01J20/18—Synthetic zeolitic molecular sieves
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40043—Purging
    • B01D2259/4005—Nature of purge gas
    • B01D2259/40052—Recycled product or process gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2259/00—Type of treatment
    • B01D2259/40—Further details for adsorption processes and devices
    • B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
    • B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
    • B01D2259/4006—Less than four
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems

Definitions

  • the described technology relates generally to an ethanol dehydration device of a multi-tube type using pressure swing adsorption process, and particularly, to an ethanol dehydration device of a multi-tube type using pressure swing adsorption process that alternately produces a dehydrated product and recycles an adsorbent in one bed by a multi-tube system.
  • anhydrous ethanol is produced by dehydrating ethanol using at least two dehydration beds in which dehydrated ethanol is produced in one bed while an adsorbent is regenerated in the other bed using vacuum and a portion of the obtained product.
  • the anhydrous ethanol product is produced in a system in which the production and regeneration are repeatedly performed in at least two beds.
  • One aspect of the present invention provides an ethanol dehydration device of a multi-tube type using pressure swing adsorption process such that heat transfer efficiency and productivity are improved.
  • an ethanol dehydration device of a multi-tube type using pressure swing adsorption process including:
  • an ethanol dehydration device of a multi-tube type using pressure swing adsorption process including:
  • the ethanol dehydration device of a multi-tube type using pressure swing adsorption process may effectively transfer heat and improve productivity, so it is possible to save the cost of early investment along with decreasing the installation charge and site of a dehydration bed.
  • FIG. 1 is a schematic view showing a pressure swing adsorption dehydration device according to one embodiment.
  • FIG. 2 and FIG. 3 are schematic views showing a multi-tube type of bed according to one embodiment.
  • FIG. 1 is a schematic view showing a pressure swing adsorption dehydration device according to one embodiment.
  • FIG. 2 and FIG. 3 show schematic views showing a multi-tube type bed according to one embodiment, which has one bed 8 having a multi-tube inside thereof.
  • the gas flow passes from the first inlet 12 through the inside 11 of the tube 10 and is adsorbed, and it simultaneously produces a dehydrated ethanol product that flows out through a first outlet 14.
  • a portion of the gas flow of the obtained product flows in through the second inlet 16 and passes through the outside 9 of the tube 10 to regenerate the absorbent, and a water/ethanol mixture having a relatively low con- centration, which is 80 to 85 volume% of ethanol, flows out through the second outlet 18.
  • a gaseous water/ethanol mixture is passed from the first inlet 12 to the first outlet 14 as the flow order in FIG. 2, so it may be absorbed at the inside 11 of the tube 10; furthermore, it is passed from the first inlet 32 to the first outlet 34 as the flow order in FIG. 3, so it may be absorbed at the outside 9 of the tube 10.
  • the dehydrated ethanol is passed from a second inlet 16 to a second outlet
  • a adsorbent is regenerated at the outside 9 of a tube 10; furthermore, it is passed from a second inlet 36 to a second outlet 38 as the flow order in FIG. 3, so the absorbent may be regenerated at the inside 11 of a tube 10.
  • the adsorption is effectively performed under the low temperature and high pressure and the desorption is effectively performed under the high temperature and low pressure in the multi-tube type bed according to the present invention.
  • the adsorption is performed under a pressure of 0.1 to
  • the absorbing at the inside of a tube and the regenerating at the outside of a tube may be alternately performed in the multi-tube type bed according to a present invention; on the other hand, the generating at the inside of tube and the absorbing at the outside of a tube may also be alternately performed.
  • the high temperature gaseous water/ethanol mixture supplied into the bed effectively transfers the heat.
  • the heat source generated by adsorbing the high temperature gaseous mixture induces the heat transfer phenomenon by the multi-tube according to the present invention.
  • it also supplies the heat source to the absorbent during the regeneration to increase the regenerativity. As a result, energy is saved.
  • the gaseous water/ethanol mixture flowing in the first inlet 12 in FIG. 2 and the first inlet 32 in FIG. 3 includes 80 to 95 volume% of ethanol.
  • the dehydrated ethanol flowing out through the first outlet 14 and the first outlet 34 has a high ethanol concentration of 99.5 volume% or more.
  • the multi-tube type bed may have 2 to 10 tubes.
  • the absorbent is Zeolite 3A or 4A.
  • the volume of the inside 11 of the tube 10 of the multi-tube type bed charged with the absorbent is the same as that of the outside 9.
  • the charged absorbent has a weight ratio of the outside 9 to the inside 11 of the tube 10 of 0.5 to 2.0.
  • the pressure swing adsorption dehydration device may include 1 to 5 multi-type type beds 8 according to the present invention.
  • the multi-tube type bed may be usable for a pre- adsorption process, a post-adsorption process, or both a pre- adsorption process and a post-adsorption process.
  • the pre-adsorption process refers to a process of producing 99.5 volume% or more of a product that is concentrated by a single-top (using one column) concentration process instead of the multi-top (using two or three columns) concentration process during the distillation process, including pre-concentrating 80 to 90 volume% of crude ethanol into 92 to 95 volume% using the multi-tube type bed and dehydrating the ethanol using the conventional two beds.
  • the post- adsorption process refers to a process of producing a product by dehydrating 92 to 96 volume% of the concentrated ethanol obtained from the pre- adsorption process and the multi-top distillation process into 99.5 volume% using the multi-tube type bed.
  • the pre-adsorption process is the same as the post- adsorption process.
  • the absorbent used in the pre- adsorption process is Zeolite 4A
  • that of post- adsorption process is Zeolite 3A.
  • Table 1 schematically illustrates a process cycle of the conventional ethanol dehydration device with pressure swing absorption process
  • Table 2 schematically illustrates a process cycle of the ethanol dehydration device of a multi-tube type using pressure swing adsorption process according to one embodiment.
  • the conventional dehydration device has two beds, of which the product is produced in one bed while the absorbent is regenerated in the other bed. These processes are repeatedly performed in the two beds.
  • the conventional dehydration device requires the total adsorption time of 3.5 to 7 minutes, which is for 0.5 to 1 minute to reduce the pressure, for 2.5 to 5 minutes to purge, and for 0.5 to 1 minute to press.
  • the purge time refers to the time for flowing in a portion of the dehydrated product to regenerate the absorbent.
  • the system includes a system including one multi-tube type bed in which producing the dehydrated product at the inside of one tube and regenerating the absorbent at the outside of tube are alternately performed, and these processes are repeatedly carried out inside and outside of the tube in one bed.
  • the dehydration device reduces the purge time to 1 to 3 minutes due to the effective heat transfer between the inside and the outside of the tube compared to the purge time of the conventional dehydration device of 2.5 to 5 minutes and increases the decompression time of 2 to 4 minutes compared to the conventional 0.5 to 1 minute, so the productivity is improved by minimizing the product amount used for the purge process.
  • the ethanol concentration is measured under normal process conditions by a moisture quantity analysis according to the Karl-Fisher method.
  • the normal process conditions refers to process conditions in which the product produced from continuously driving the ethanol dehydration device of a multi-tube type using pressure swing adsorption process is to have a concentration of 99.5 volume% or more when it is measured by the Karl-Fisher method.
  • the ethanol dehydration device of a multi-tube type using pressure swing adsorption process may effectively transfer heat and improve productivity, so it is possible to save the cost of early investment along with decreasing the installation charge and site of a dehydration bed.

Abstract

Disclosed is an ethanol dehydration device of a multi-tube type using pressure swing adsorption process in which producing dehydrated ethanol and regenerating an absorbent are alternately performed in one bed having a multi-tube. The dehydration device effectively transfers heat since it has a multi-tube type bed and minimizes heat loss by using a heat source generated during the absorption. Thereby, it improves the regeneration of absorbent and productivity. In addition, it is possible to save the early investment cost due to decreasing the installation cost and site of the dehydration bed.

Description

ETHANOL DEHYDRATION DEVICE OF MULTI-TUBE TYPE USING PRESSURE SWING ADSORPTION PROCESS
The described technology relates generally to an ethanol dehydration device of a multi-tube type using pressure swing adsorption process, and particularly, to an ethanol dehydration device of a multi-tube type using pressure swing adsorption process that alternately produces a dehydrated product and recycles an adsorbent in one bed by a multi-tube system.
Generally, anhydrous ethanol is produced by dehydrating ethanol using at least two dehydration beds in which dehydrated ethanol is produced in one bed while an adsorbent is regenerated in the other bed using vacuum and a portion of the obtained product.
In this way, the anhydrous ethanol product is produced in a system in which the production and regeneration are repeatedly performed in at least two beds.
During the process, attention should be paid to keep each bed warm and to externally radiate heat. Particularly, the high-temperature gaseous water/ethanol mixture supplied to the dehydration bed somewhat deteriorates the process efficiency since it is difficult to effectively transfer heat.
One aspect of the present invention provides an ethanol dehydration device of a multi-tube type using pressure swing adsorption process such that heat transfer efficiency and productivity are improved.
According to one aspect of the present invention provides an ethanol dehydration device of a multi-tube type using pressure swing adsorption process, including:
a plurality of tubes of which an absorbent is charged inside and outside thereof;
a plurality of first inlets disposed in an upper end of each tube and into which a gaseous water/ethanol mixture flows;
a plurality of first outlets disposed on a lower end of the tube and from which dehydrated ethanol flows, wherein the ethanol is dehydrated by an absorbent by passing the gaseous water/ethanol mixture flowing into the first inlets through the inside of the tube;
a plurality of second inlets disposed between the first inlet and the first outlet and through which the dehydrated ethanol coming from the first outlet flows; and
a plurality of second outlets disposed between the first inlet and the first outlet and through which a gaseous water/ethanol mixture flows, wherein the gaseous water/ethanol mixture is formed by passing the dehydrated ethanol flowing in the second inlet through the outside of the tube to regenerate the absorbent absorbing moisture.
According to another aspect of the present invention provides an ethanol dehydration device of a multi-tube type using pressure swing adsorption process, including:
a plurality of tubes charged with an absorbent at the inside and outside thereof;
a plurality of first inlets disposed on one side surface of the tube and through which a gaseous water/ethanol mixture flows;
a plurality of first outlets disposed on the other side surface of the tube and through which dehydrated ethanol flows, wherein the ethanol is dehydrated by an absorbent by passing the gaseous water/ethanol mixture flowing in the first inlets through the outside of the tube;
a plurality of second inlets disposed in the lower end of tube and through which the dehydrated ethanol coming from the first outlet flows; and
a plurality of second outlets disposed on the upper end of the tube and through which a gaseous water/ethanol mixture flows, wherein the gaseous water/ethanol mixture is formed by passing the dehydrated ethanol flowing in the second inlet through the inside of the tube to regenerate the absorbent absorbing moisture.
The ethanol dehydration device of a multi-tube type using pressure swing adsorption process may effectively transfer heat and improve productivity, so it is possible to save the cost of early investment along with decreasing the installation charge and site of a dehydration bed.
FIG. 1 is a schematic view showing a pressure swing adsorption dehydration device according to one embodiment.
FIG. 2 and FIG. 3 are schematic views showing a multi-tube type of bed according to one embodiment.
<Description of Reference Numerals Indicating Primary Elements in the Drawings>
2: crude ethanoll reservoir 4: heater
6, 20: 4-way valve 8: multi-tube type bed
9: outside of tube 10: tube
11: inside of tube 12, 32: first inlet
14, 34: first outlet 16, 36: second inlet
18, 38: second outlet 22: product reservoir
24: vacuum pump
Exemplary embodiments will hereinafter be described in detail. However, these embodiments are only exemplary, and the present invention is not limited thereto. The present invention may, however, be embodied in many different forms and should not be construed as limited to the exemplary embodiments set forth herein.
FIG. 1 is a schematic view showing a pressure swing adsorption dehydration device according to one embodiment.
As shown in FIG. 1, crude ethanol having a moisture concentration of 5 to 15 volume% stored in a crude ethanol reservoir 2 is moved to a heater 4 and heated to about 130 to 140℃. Then the crude ethanol having passed through 4-way valve 6 is passed into a multi-tube type bed 8 to produce dehydrated ethanol and to regenerate absorbent. The dehydrated ethanol product is passed through a 4-way valve 20 and moved into a product reservoir 22. On the other hand, a portion of the dehydrated ethanol product is drawn into a reservoir (not shown) and maintained under vacuum by a vacuum pump 24 in order to regenerate the absorbent.
In other words, producing the product and regenerating the absorbent are alternately performed in one bed in which a multi-tube is mounted, and the multi-tube type bed 8 will now be described with reference to FIG. 2 and FIG. 3.
FIG. 2 and FIG. 3 show schematic views showing a multi-tube type bed according to one embodiment, which has one bed 8 having a multi-tube inside thereof.
Firstly, when the crude ethanol, which is a gaseous water/ethanol mixture, flows in a first inlet 12 and is passed through the inside 11 of a tube 10 disposed in the bed 8, it is dehydrated by an absorbent charged in the inside 11 of the tube 10 and flows out through a first outlet 14 to provide a dehydrated ethanol product having high purity. A portion of the obtained dehydrated ethanol product flows in a second inlet 16 and is passed through the outside 9 of the tube 10 disposed in the bed 8 to regenerate the absorbent used for dehydrating ethanol. The adsorbed moisture is bound with the ethanol supplied from the second inlet 16 to provide a water/ethanol mixture and flows out through a second outlet 18.
That is, the gas flow passes from the first inlet 12 through the inside 11 of the tube 10 and is adsorbed, and it simultaneously produces a dehydrated ethanol product that flows out through a first outlet 14. A portion of the gas flow of the obtained product flows in through the second inlet 16 and passes through the outside 9 of the tube 10 to regenerate the absorbent, and a water/ethanol mixture having a relatively low concentration, which is 80 to 85 volume% of ethanol, flows out through the second outlet 18.
Furthermore, when the product is produced and the absorbent is regenerated during the process, the gas flow is changed by the 4-way valves 6 and 20.
That is, as shown in FIG. 3, when a gaseous water/ethanol mixture flows in through a first inlet 32 and passes through the outside 9 of a tube disposed in the bed 8, it is dehydrated by an absorbent charged at the outside 9 of the tube 10 and flows out through a first outlet 34 to provide dehydrated ethanol. When a portion of the obtained dehydrated ethanol product flows in a second inlet 36 and passes through the inside 11 of the tube 10 disposed in the bed 8, the water-absorbed absorbent is regenerated, and simultaneously the obtained gaseous water/ethanol mixture flows out through a second outlet 38.
In other words, when the gas flow passes through the outside 9 of the tube 10 from the first inlet 32 to the first outlet 34, it is adsorbed, and simultaneously the dehydrated ethanol is produced; and when a portion of gas flow of the product is passed through the inside 11 of the tube 10 from the second inlet 36 to the second outlet 38, the absorbent is regenerated.
As shown in FIG. 2 and FIG. 3, collectively looking at the embodiment, a gaseous water/ethanol mixture is passed from the first inlet 12 to the first outlet 14 as the flow order in FIG. 2, so it may be absorbed at the inside 11 of the tube 10; furthermore, it is passed from the first inlet 32 to the first outlet 34 as the flow order in FIG. 3, so it may be absorbed at the outside 9 of the tube 10.
In addition, the dehydrated ethanol is passed from a second inlet 16 to a second outlet 18 as the flow order in FIG. 2, so a adsorbent is regenerated at the outside 9 of a tube 10; furthermore, it is passed from a second inlet 36 to a second outlet 38 as the flow order in FIG. 3, so the absorbent may be regenerated at the inside 11 of a tube 10.
According to one embodiment, the adsorption is effectively performed under the low temperature and high pressure and the desorption is effectively performed under the high temperature and low pressure in the multi-tube type bed according to the present invention.
According to one embodiment, the adsorption is performed under a pressure of 0.1 to 0.6 ㎏/cm2, and the desorption is performed under a pressure of -0.5 to -0.9 ㎏/cm2 in a bed.
As mentioned above, the absorbing at the inside of a tube and the regenerating at the outside of a tube may be alternately performed in the multi-tube type bed according to a present invention; on the other hand, the generating at the inside of tube and the absorbing at the outside of a tube may also be alternately performed. Thereby, the high temperature gaseous water/ethanol mixture supplied into the bed effectively transfers the heat.
In other words, the heat source generated by adsorbing the high temperature gaseous mixture induces the heat transfer phenomenon by the multi-tube according to the present invention. In addition, it also supplies the heat source to the absorbent during the regeneration to increase the regenerativity. As a result, energy is saved.
The gaseous water/ethanol mixture flowing in the first inlet 12 in FIG. 2 and the first inlet 32 in FIG. 3 includes 80 to 95 volume% of ethanol. The dehydrated ethanol flowing out through the first outlet 14 and the first outlet 34 has a high ethanol concentration of 99.5 volume% or more.
According to one embodiment, the multi-tube type bed may have 2 to 10 tubes.
The absorbent is Zeolite 3A or 4A.
In addition, according to one embodiment, the volume of the inside 11 of the tube 10 of the multi-tube type bed charged with the absorbent is the same as that of the outside 9. According to another embodiment, the charged absorbent has a weight ratio of the outside 9 to the inside 11 of the tube 10 of 0.5 to 2.0.
The pressure swing adsorption dehydration device may include 1 to 5 multi-type type beds 8 according to the present invention.
In addition, the multi-tube type bed may be usable for a pre-adsorption process, a post-adsorption process, or both a pre-adsorption process and a post-adsorption process.
The pre-adsorption process refers to a process of producing 99.5 volume% or more of a product that is concentrated by a single-top (using one column) concentration process instead of the multi-top (using two or three columns) concentration process during the distillation process, including pre-concentrating 80 to 90 volume% of crude ethanol into 92 to 95 volume% using the multi-tube type bed and dehydrating the ethanol using the conventional two beds.
The post-adsorption process refers to a process of producing a product by dehydrating 92 to 96 volume% of the concentrated ethanol obtained from the pre-adsorption process and the multi-top distillation process into 99.5 volume% using the multi-tube type bed.
In the view of the process cycle, the pre-adsorption process is the same as the post-adsorption process. According to one embodiment, the absorbent used in the pre-adsorption process is Zeolite 4A, and that of post-adsorption process is Zeolite 3A.
The following Table 1 schematically illustrates a process cycle of the conventional ethanol dehydration device with pressure swing absorption process, and the following Table 2 schematically illustrates a process cycle of the ethanol dehydration device of a multi-tube type using pressure swing adsorption process according to one embodiment.
Table 1
Figure PCTKR2009004886-appb-T000001
Table 2
Figure PCTKR2009004886-appb-T000002
As shown in Table 1, the conventional dehydration device has two beds, of which the product is produced in one bed while the absorbent is regenerated in the other bed. These processes are repeatedly performed in the two beds.
In addition, the conventional dehydration device requires the total adsorption time of 3.5 to 7 minutes, which is for 0.5 to 1 minute to reduce the pressure, for 2.5 to 5 minutes to purge, and for 0.5 to 1 minute to press.
The purge time refers to the time for flowing in a portion of the dehydrated product to regenerate the absorbent.
On the other hand, it includes a system including one multi-tube type bed in which producing the dehydrated product at the inside of one tube and regenerating the absorbent at the outside of tube are alternately performed, and these processes are repeatedly carried out inside and outside of the tube in one bed.
Furthermore, the dehydration device reduces the purge time to 1 to 3 minutes due to the effective heat transfer between the inside and the outside of the tube compared to the purge time of the conventional dehydration device of 2.5 to 5 minutes and increases the decompression time of 2 to 4 minutes compared to the conventional 0.5 to 1 minute, so the productivity is improved by minimizing the product amount used for the purge process.
On the other hand, when Zeolite 3A is used as the adsorbent, the dehydrated ethanol concentration and the ethanol concentration of the gaseous water/ethanol mixture flowing out during regeneration of the adsorbent are shown in the following Table 3.
The ethanol concentration is measured under normal process conditions by a moisture quantity analysis according to the Karl-Fisher method. The normal process conditions refers to process conditions in which the product produced from continuously driving the ethanol dehydration device of a multi-tube type using pressure swing adsorption process is to have a concentration of 99.5 volume% or more when it is measured by the Karl-Fisher method.
Table 3
Figure PCTKR2009004886-appb-T000003
The ethanol dehydration device of a multi-tube type using pressure swing adsorption process may effectively transfer heat and improve productivity, so it is possible to save the cost of early investment along with decreasing the installation charge and site of a dehydration bed.

Claims (7)

  1. An ethanol dehydration device of a multi-tube type using pressure swing adsorption process, comprising:
    a plurality of tubes of which an absorbent is charged inside and outside thereof;
    a plurality of first inlets disposed in an upper end of each tube and into which a gaseous water/ethanol mixture flows;
    a plurality of first outlets disposed on a lower end of the tube and from which dehydrated ethanol flows, wherein the ethanol is dehydrated by an absorbent by passing the gaseous water/ethanol mixture flowing into the first inlets through the inside of the tube;
    a plurality of second inlets disposed between the first inlet and the first outlet and through which the dehydrated ethanol coming from the first outlet flows; and
    a plurality of second outlets disposed between the first inlet and the first outlet and through which a gaseous water/ethanol mixture flows, wherein the gaseous water/ethanol mixture is formed by passing the dehydrated ethanol flowing in the second inlet through the outside of the tube to regenerate the absorbent absorbing moisture.
  2. The dehydration device of claim 1, wherein 2 to 10 tubes are present in the multi-tube type bed.
  3. The dehydration device of claim 1, wherein the absorbent is Zeolite 3A or 4A.
  4. The dehydration device of claim 1, wherein the absorbent has a weight ratio of outside of the tube to the inside the tube of 0.5 to 2.0.
  5. The dehydration device of claim 1, comprising 1 to 5 multi-tube beds.
  6. The dehydration device of claim 1, wherein the dehydrated ethanol comprises 99.5 volume% or more of ethanol.
  7. An ethanol dehydration device of a multi-tube type using pressure swing absorption process, comprising:
    a plurality of tubes charged with an absorbent inside and outside thereof;
    a plurality of first inlets disposed on one side surface of the tube and through which a gaseous water/ethanol mixture flows;
    a plurality of first outlets disposed on the other side surface of the tube and through which dehydrated ethanol flows, wherein the ethanol is dehydrated by an absorbent by passing the gaseous water/ethanol mixture flowing in the first inlets through the outside of the tube;
    a plurality of second inlets disposed on the lower end of tube and through which the dehydrated ethanol coming from the first outlet flows; and
    a plurality of second outlets disposed on the upper end of the tube and through which a gaseous water/ethanol mixture flows, wherein the gaseous water/ethanol mixture is formed by passing the dehydrated ethanol flowing in the second inlet through the inside of the tube to regenerate the absorbent absorbing moisture.
PCT/KR2009/004886 2008-09-01 2009-08-31 Ethanol dehydration device of multi-tube type using pressure swing adsorption process WO2010024643A1 (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020080085955A KR101062918B1 (en) 2008-09-01 2008-09-01 Multitube Type Ethanol Pressure Swing Adsorption Dewatering Device
KR10-2008-0085955 2008-09-01

Publications (1)

Publication Number Publication Date
WO2010024643A1 true WO2010024643A1 (en) 2010-03-04

Family

ID=41721666

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2009/004886 WO2010024643A1 (en) 2008-09-01 2009-08-31 Ethanol dehydration device of multi-tube type using pressure swing adsorption process

Country Status (2)

Country Link
KR (1) KR101062918B1 (en)
WO (1) WO2010024643A1 (en)

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018044501A1 (en) 2016-09-01 2018-03-08 Exxonmobil Upstream Research Company Swing adsorption processes for removing water using 3a zeolite structures
US10675615B2 (en) 2014-11-11 2020-06-09 Exxonmobil Upstream Research Company High capacity structures and monoliths via paste imprinting
US10744449B2 (en) 2015-11-16 2020-08-18 Exxonmobil Upstream Research Company Adsorbent materials and methods of adsorbing carbon dioxide
US11033854B2 (en) 2016-05-31 2021-06-15 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11033852B2 (en) 2016-05-31 2021-06-15 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11110388B2 (en) 2016-08-31 2021-09-07 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
US11148091B2 (en) 2016-12-21 2021-10-19 Exxonmobil Upstream Research Company Self-supporting structures having active materials
US11260339B2 (en) 2016-03-18 2022-03-01 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
US11318410B2 (en) 2018-12-21 2022-05-03 Exxonmobil Upstream Research Company Flow modulation systems, apparatus, and methods for cyclical swing adsorption
US11331620B2 (en) 2018-01-24 2022-05-17 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11376545B2 (en) 2019-04-30 2022-07-05 Exxonmobil Upstream Research Company Rapid cycle adsorbent bed
US11413567B2 (en) 2018-02-28 2022-08-16 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11433346B2 (en) 2019-10-16 2022-09-06 Exxonmobil Upstream Research Company Dehydration processes utilizing cationic zeolite RHO
US11655910B2 (en) 2019-10-07 2023-05-23 ExxonMobil Technology and Engineering Company Adsorption processes and systems utilizing step lift control of hydraulically actuated poppet valves
US11707729B2 (en) 2016-12-21 2023-07-25 ExxonMobil Technology and Engineering Company Self-supporting structures having active materials

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101700220B1 (en) 2015-07-08 2017-01-31 (주)파인텍 The ethanol dehydration system

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2265473C1 (en) * 2004-07-09 2005-12-10 Закрытое акционерное общество Научно-производственное объединение "Химсинтез" Method of production of a dehydrated ethyl alcohol
WO2007047622A1 (en) * 2005-10-18 2007-04-26 Archer-Daniels-Midland Company Regenerating molecular sieve absorbents used for ethanol dehydration
FR2907023A1 (en) * 2006-10-17 2008-04-18 Maguin Sas Dehydration of water/alcohol e.g. ethanol mixture, comprises vaporizing/overheating the mixture, passing the mixture to a vapor over a molecular sieve for provoking the adsorption of water, and condensing a dehydrated alcohol vapor

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS5881422A (en) 1981-11-11 1983-05-16 Hidenobu Toyotomi Adsorptive separation of air
JPS60129116A (en) 1983-12-16 1985-07-10 Kobe Steel Ltd Adsorbing device regenerable without heating

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2265473C1 (en) * 2004-07-09 2005-12-10 Закрытое акционерное общество Научно-производственное объединение "Химсинтез" Method of production of a dehydrated ethyl alcohol
WO2007047622A1 (en) * 2005-10-18 2007-04-26 Archer-Daniels-Midland Company Regenerating molecular sieve absorbents used for ethanol dehydration
FR2907023A1 (en) * 2006-10-17 2008-04-18 Maguin Sas Dehydration of water/alcohol e.g. ethanol mixture, comprises vaporizing/overheating the mixture, passing the mixture to a vapor over a molecular sieve for provoking the adsorption of water, and condensing a dehydrated alcohol vapor

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10675615B2 (en) 2014-11-11 2020-06-09 Exxonmobil Upstream Research Company High capacity structures and monoliths via paste imprinting
US11642619B2 (en) 2015-11-16 2023-05-09 Georgia Tech Research Corporation Adsorbent materials and methods of adsorbing carbon dioxide
US10744449B2 (en) 2015-11-16 2020-08-18 Exxonmobil Upstream Research Company Adsorbent materials and methods of adsorbing carbon dioxide
US11260339B2 (en) 2016-03-18 2022-03-01 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
US11033852B2 (en) 2016-05-31 2021-06-15 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11033854B2 (en) 2016-05-31 2021-06-15 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11110388B2 (en) 2016-08-31 2021-09-07 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes related thereto
US11318413B2 (en) 2016-09-01 2022-05-03 Exxonmobil Upstream Research Company Swing adsorption processes using zeolite structures
CN109922872A (en) * 2016-09-01 2019-06-21 埃克森美孚上游研究公司 Use the zeolite structured variation adsorption treatment for removing water of 3A
WO2018044501A1 (en) 2016-09-01 2018-03-08 Exxonmobil Upstream Research Company Swing adsorption processes for removing water using 3a zeolite structures
US10603626B2 (en) 2016-09-01 2020-03-31 Exxonmobil Upstream Research Company Swing adsorption processes using zeolite structures
AU2017320837B2 (en) * 2016-09-01 2020-07-23 Exxonmobil Upstream Research Company Swing adsorption processes for removing water using 3A zeolite structures
US11148091B2 (en) 2016-12-21 2021-10-19 Exxonmobil Upstream Research Company Self-supporting structures having active materials
US11707729B2 (en) 2016-12-21 2023-07-25 ExxonMobil Technology and Engineering Company Self-supporting structures having active materials
US11331620B2 (en) 2018-01-24 2022-05-17 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11857913B2 (en) 2018-01-24 2024-01-02 ExxonMobil Technology and Engineering Company Apparatus and system for swing adsorption processes
US11413567B2 (en) 2018-02-28 2022-08-16 Exxonmobil Upstream Research Company Apparatus and system for swing adsorption processes
US11318410B2 (en) 2018-12-21 2022-05-03 Exxonmobil Upstream Research Company Flow modulation systems, apparatus, and methods for cyclical swing adsorption
US11376545B2 (en) 2019-04-30 2022-07-05 Exxonmobil Upstream Research Company Rapid cycle adsorbent bed
US11655910B2 (en) 2019-10-07 2023-05-23 ExxonMobil Technology and Engineering Company Adsorption processes and systems utilizing step lift control of hydraulically actuated poppet valves
US11433346B2 (en) 2019-10-16 2022-09-06 Exxonmobil Upstream Research Company Dehydration processes utilizing cationic zeolite RHO

Also Published As

Publication number Publication date
KR101062918B1 (en) 2011-09-06
KR20100026808A (en) 2010-03-10

Similar Documents

Publication Publication Date Title
WO2010024643A1 (en) Ethanol dehydration device of multi-tube type using pressure swing adsorption process
TWI552957B (en) Co2 adsorption and recovery system and method
CN110174020A (en) A kind of heat exchanger of unsymmetrical arrangement
WO2015062341A1 (en) Adsorbing and drying device
CN201404756Y (en) Tee-valve closed cycle heating regenerative gas dryer
CN106512644A (en) Multi-layer adsorption tower for purifying electronic grade polycrystalline silicon tail gas
CN111411004A (en) Method and device for efficiently purifying biogas by using pressure swing adsorption principle
CN203577571U (en) Regeneration blow-cooling pipeline system for adsorption cylinder of air purifier
CN101601959A (en) A kind of Zero gas consumption low dew point compression heat regeneration absorption compressed air drying method and device thereof
CN108373144A (en) A kind of thick neon helium is refined to remove hydrogen system
CN115554808A (en) Industrial waste gas decarbonization device
CN100479903C (en) Active carbon fiber fixed bed continuous adsorption and desorption apparatus
CN110118360B (en) Synergistic flue gas waste heat utilization system and carbon-based loaded ionic liquid desulfurization method
CN211216062U (en) Active carbon continuous replacing system
CN110218858B (en) Lead-containing waste gas treatment device for lead quenching in steel wire production
CN113931256A (en) Energy-saving method and system for controlling environment humidity and producing water from air
CN103449968B (en) Isopropanol refined raw material absorption-rectification coupling apparatus and methods and applications
WO2013102344A1 (en) Adsorption dryer
CN206613354U (en) Low-grade fever regenerative adsorptive drier
CN213725677U (en) Adsorption drying tower
CN213119141U (en) Waste heat recovery device for heat supply boiler
CN2907847Y (en) Air purification drier
CN219441165U (en) Adsorption regeneration device for waste gas treatment
WO2013100306A1 (en) Method for manufacturing a carbon dioxide adsorbent, method for reducing carbon dioxide and apparatus for same
CN211513986U (en) Waste gas active carbon adsorption desorption device

Legal Events

Date Code Title Description
WWE Wipo information: entry into national phase

Ref document number: 12010500797

Country of ref document: PH

121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 09810248

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 09810248

Country of ref document: EP

Kind code of ref document: A1