AU2021104798A4 - Countercurrent Exchange Membrane Distillation Device - Google Patents
Countercurrent Exchange Membrane Distillation Device Download PDFInfo
- Publication number
- AU2021104798A4 AU2021104798A4 AU2021104798A AU2021104798A AU2021104798A4 AU 2021104798 A4 AU2021104798 A4 AU 2021104798A4 AU 2021104798 A AU2021104798 A AU 2021104798A AU 2021104798 A AU2021104798 A AU 2021104798A AU 2021104798 A4 AU2021104798 A4 AU 2021104798A4
- Authority
- AU
- Australia
- Prior art keywords
- hollow fiber
- fiber membrane
- groups
- hollow tube
- cylindrical shell
- 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.)
- Active
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 153
- 238000004821 distillation Methods 0.000 title claims abstract description 41
- 239000012510 hollow fiber Substances 0.000 claims abstract description 87
- 239000002351 wastewater Substances 0.000 claims abstract description 73
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 37
- 239000011780 sodium chloride Substances 0.000 claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 21
- 238000011282 treatment Methods 0.000 claims abstract description 16
- 238000010521 absorption reaction Methods 0.000 claims abstract description 14
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 65
- 229910021529 ammonia Inorganic materials 0.000 claims description 32
- 238000000034 method Methods 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 6
- 239000011148 porous material Substances 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- 239000012466 permeate Substances 0.000 claims description 2
- 238000009834 vaporization Methods 0.000 claims description 2
- 230000008016 vaporization Effects 0.000 claims description 2
- 230000000694 effects Effects 0.000 abstract description 7
- 238000007789 sealing Methods 0.000 abstract description 6
- 239000013535 sea water Substances 0.000 abstract description 4
- 230000009615 deamination Effects 0.000 abstract description 3
- 238000006481 deamination reaction Methods 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 238000000926 separation method Methods 0.000 description 8
- 239000004743 Polypropylene Substances 0.000 description 6
- -1 polypropylene Polymers 0.000 description 6
- 229920001155 polypropylene Polymers 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000010612 desalination reaction Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive effect Effects 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000003723 Smelting Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000012982 microporous membrane Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 238000003911 water pollution Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/447—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by membrane distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/364—Membrane distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/366—Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/02—Hollow fibre modules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/02—Details relating to pores or porosity of the membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2325/00—Details relating to properties of membranes
- B01D2325/02—Details relating to pores or porosity of the membranes
- B01D2325/0283—Pore size
- B01D2325/02834—Pore size more than 0.1 and up to 1 µm
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a countercurrent exchange membrane distillation device, which
comprises a cylindrical shell, an absorption liquid inlet, a distillate outlet, an upper circular
head and a lower circular head. At least 5 groups of hollow tube groups, at least 5 groups of
hollow fiber membrane groups and a grid screen for separating the hollow tube groups and the
hollow fiber membrane groups are arranged in the cylindrical shell. The absorption liquid inlet
is arranged on the upper side wall of the cylindrical shell, the distillate outlet is arranged on the
lower side wall of the cylindrical shell, and the upper circular head and the lower circular head
are connected with the cylindrical shell through concave-convex flanges. The upper circular
head is provided with a hollow fiber membrane group feed port and a hollow tube group
discharge port, and the lower circular head is provided with a hollow fiber membrane group
discharge port and a hollow tube group feed port. The invention has the advantages of simple
structure, good sealing effect, convenient operation and high heat transfer efficiency. It is
convenient to be applied in recycling occasions such as sea water desalinization, industrial
saline wastewater, membrane deamination and the like, and realizes industrial popularization.
2/2
External heat transfer
Saline wastewater Saline wastewater to
after treatment be treatm ent
Figure 3
Description
2/2
External heat transfer
Saline wastewater Saline wastewater to after treatment be treatm ent
Figure 3
Countercurrent Exchange Membrane Distillation Device
The invention relates to a countercurrent exchange membrane distillation device and a
treatment method thereof for saline wastewater and ammonia-containing wastewater,
belonging to the technical field of membrane separation.
China is a country with serious shortage of water resources. The lack of water resources
and increasingly serious water pollution have seriously affected people's lives and social
development. Saline wastewater and ammonia nitrogen wastewater are two common
types of wastewater at present. Saline wastewater mainly comes from seawater
desalination and coal chemical production. Ammonia nitrogen wastewater comes from
fine chemical industry, chemical fertilizer, coal chemical industry, pharmacy, pesticide,
nonferrous metal smelting and other fields, and is an important substance for water
eutrophication and environmental pollution. At present, saline wastewater is mainly
reused by membrane separation technology, which has the advantages of simple process,
less land occupation, excellent effluent quality, no suspended solids, direct reuse and less
excess sludge. Ammonia-containing wastewater is generally treated by biological
method, which has stable treatment effect, does not produce secondary pollution, and is
economical, but has the disadvantages of large occupied area, low efficiency at low
temperature, easy to be affected by toxic substances and troublesome operation and
management. With the development of membrane technology, gas-water separation
membrane distillation (MD) technology emerged, which is a membrane separation
process combining membrane technology with distillation process. It uses hydrophobic microporous membrane as medium, and under the action of vapor pressure difference on both sides of the membrane, volatile components in the solution pass through the membrane pores in vapor form, thus realizing separation. Compared with other commonly used separation processes, membrane distillation has the advantages of high separation efficiency and mild operating conditions, and is a new and effective membrane separation technology, which has a good treatment effect on saline wastewater and ammonia-containing wastewater.
The utility model patent entitled "A Membrane Distiller" (publication number
CN103710245A) discloses a membrane distiller. It comprises a rectangular shell, wherein
the upper and lower ends of the shell are respectively an upper cover plate and a lower
cover plate, a feed liquid inlet and outlet are arranged on the upper and lower cover
plates, a distillate outlet is arranged on the lower part of the shell, a membrane module is
arranged in the cavity of the shell, and the shell cavity is divided into three sections.
Wherein partition plates with the same direction are respectively arranged in the upper
and lower cavities to form a symmetrical double-cavity structure, a communicated single
cavity is arranged between the upper and lower cavities, at least two rows of hollow fiber
membrane module units are fixed by adhesive in the same side cavity of the upper and
lower cavities, and at least two rows of hollow tube module units are fixed by adhesive in
the other same side cavity of the upper and lower cavities. The single cavity between the
upper cavity and the lower cavity is filled with membrane modules alternately arranged
between hollow fiber membrane module units and hollow tube module units, and a screen
arranged between adjacent hollow fiber membrane module units and hollow tube module
units. The above-mentioned membrane distiller structure has the following shortcomings.
(1) The rectangular shell is prone to corner dead flow, which is not conducive to the
renewal and exchange of gas and liquid, and is not suitable for the quantitative production
and installation of later industrial popularization. (2) The hollow fiber membrane module
units and the hollow tube module units are arranged on the same side, leading to the
phenomenon of parallel flow and wall flow, resulting in the situation of low gas-liquid
heat transfer efficiency and poor mass transfer effect.
Object of the invention: In order to overcome the shortcomings of the prior art, the
invention provides a countercurrent exchange membrane distillation device with simple
manufacture and good sealing performance. At the same time, it also provides the
treatment method of saline wastewater and ammonia-containing wastewater. The method
has mild operation conditions, simple operation process, high heat utilization efficiency
and wide application range.
Technical scheme: the countercurrent exchange membrane distillation device according
to the invention comprises a cylindrical shell, an absorption liquid inlet, a distillate outlet,
an upper circular head and a lower circular head. The cavity in the cylindrical shell is
divided into upper, middle and lower parts, the upper and lower cavities are respectively
provided with partition plates to divide them into symmetrical inner cavity structures, the
middle cavity is communicated with the inner cavities of the upper and lower cavities, at
least 5 hollow tube groups are arranged in two inner cavities on different sides of the
upper and lower cavities, and at least 5 hollow fiber membrane groups are arranged in
two inner cavities on different sides of the upper and lower cavities. A Grid screen is
arranged in the middle cavity to separate the hollow tube group and the hollow fiber membrane group, so that the hollow tube group and the hollow fiber membrane group are arranged alternately. The absorption liquid inlet is arranged at the upper part of the side wall of the middle cavity, the distillate outlet is arranged at the lower part of the side wall of the middle cavity, the upper circular head is connected with the top end of the cylindrical shell through a concave-convex flange, and the lower circular head is connected with the bottom end of the cylindrical shell through a concave-convex flange.
The upper circular head is provided with a hollow fiber membrane group feed port
communicating with hollow fiber membrane groups and a hollow tube group discharge
port communicating with hollow fiber membrane groups. The lower circular head is
provided with a hollow fiber membrane group discharge port communicating with the
hollow fiber membrane groups and a hollow tube group feed port communicating with
the hollow tube groups.
Further improving the technical scheme, the hollow tube group and the hollow fiber
membrane group in the middle cavity are arranged in an X-shaped cross.
The main structural characteristics of the membrane distillation device are as follows.
The hollow fiber membrane group consists of 100-800 hollow fiber membranes with
inner diameter of 0.2-1 mm, wall thickness of 0.2-0.5 mm, pore diameter of 0.2-0.8 um,
porosity of 0.4-0.8 and length of 500-1800 mm in diagonal single row arrangement. The
hollow tube group consists of 100-800 hollow tubes with inner diameter of 0.2-1 mm,
wall thickness of 5-100 um and length of 500-1800 mm in diagonal single row
arrangement. The mesh number of the grid screen is 10-100. The height of that
cylindrical shell is 1000-3000 mm, the inner diameter is 50-500 mm, and the wall thickness is 4-40 mm. The heights of the upper circular head and the lower circular head are both 30 mm.
The method for treating saline wastewater by using the membrane distillation device
comprises the following steps.
(1) The saline wastewater to be treated input from the hollow tube group feed port enters
the hollow tube groups, undergoes countercurrent heat exchange with the high
temperature saline wastewater existing in the hollow fiber membrane groups, and then is
output from the hollow tube group discharge port.
(2) The preheated saline wastewater output from the hollow tube group discharge port is
further raised to the vaporization temperature after external supplementary heat exchange,
and enters the hollow fiber membrane groups in the cylindrical shell from the hollow
fiber membrane group feed port.
(3) The saline wastewater enters the hollow fiber membrane groups and the newly input
saline wastewater of the hollow tube groups undergo countercurrent heat exchange, the
heat is released, the water vapor diffuses to the gap in the cylindrical shell through the
membrane holes on the membrane wall of the hollow fiber membrane, and the permeate
is cooled to become liquid, and discharged from the distillate outlet, so that the single
stage membrane distillation process is completed.
(4) Repeat the cycle of steps (1) to (3) to complete the distillation process of a large
amount of saline wastewater.
The method for treating ammonia-containing wastewater by using the membrane
distillation device comprises the following steps.
(1) Ammonia-containing wastewater to be treated input from the hollow tube group feed
port enters the hollow tube group, undergoes countercurrent heat exchange with the high
temperature ammonia-containing wastewater existing in the hollow fiber membrane
groups, and then is output from the hollow tube group discharge port.
(2) The preheated ammonia-containing wastewater output from the hollow tube group
discharge port is further heated by external supplementary heat exchange, and enters the
hollow fiber membrane groups in the cylindrical shell from the hollow fiber membrane
group feed port.
(3) Ammonia in the ammonia-containing wastewater entering the hollow fiber membrane
groups evaporates and diffuses to the gap in the cylindrical shell through the membrane
holes on the hollow fiber membrane wall, and is absorbed and collected by the absorption
liquid added in the shell and flows out from the distillate outlet. At the same time, the
ammonia-containing wastewater and the newly input ammonia-containing wastewater of
the hollow tube groups undergo countercurrent heat exchange for preheating the newly
input ammonia-containing wastewater, so that the single-stage membrane distillation
process is completed. The absorption liquid includes but is not limited to sulfuric acid,
hydrochloric acid and nitric acid.
(4) Repeat the cycle of steps (1) to (3) to complete the distillation treatment process of a
large amount of ammonia-containing wastewater.
Compared with the prior art, the invention has the advantages as follows.
1. The grid screen ensures the regular structure between the hollow fiber membrane
group and the hollow tube group, and improves the thermal efficiency of the whole
membrane distillation process.
2. The upper circular head and the lower circular head are respectively connected with the
cylindrical shell through concave-convex flanges, enhancing the sealing performance of
the whole device.
3. The loading method of cylindrical shell is adopted. It provides a larger effective
membrane area than other methods under the same area, that is, provides a larger mass
transfer and heat transfer channel, and improves the unit effective treatment capacity. On
the other hand, it overcomes the defect of dead flow at the corner end of square shell
structure, which is not conducive to gas-liquid renewal and exchange. At the same time,
the design of the loading mode of the cylindrical shell is beneficial to the quantitative
production and installation of the later industrial popularization, and the structural layout
has a high aesthetic appearance.
4. The hollow fiber membrane group and the hollow tube group are arranged on different
sides of X-shaped structure, which forms countercurrent exchange, reduces the
phenomenon of parallel flow and wall flow, avoids the situation of low heat transfer
efficiency and poor mass transfer effect, and is more conducive to improving gas-liquid
mass transfer and heat transfer efficiency and treatment effect.
5. The membrane distillation device has the advantages of simple structure, good sealing
effect, convenient operation and high heat transfer efficiency. It is convenient to be
applied in recycling occasions such as seawater and fresh water, industrial saline
wastewater, membrane deamination and the like, thus realizing industrial popularization.
Figure 1 A schematic diagram of the device of the present invention
Among them, 1-hollow tube group feed port, 2-hollow fiber membrane group discharge
port, 3-lower circular head, 4-distillate outlet, 5-shell, 6-upper circular head, 7-hollow
tube group discharge port, 8-hollow fiber membrane group feed port and 13-absorption
liquid inlet.
Figure 2 A sectional view of the membrane distillation device of the present invention
Among them, 9-hollow fiber membrane, 10-hollow tube and 11-mesh screen.
Figure 3 A schematic diagram of the internal structure of the device and its process for
treating saline wastewater.
Among them, 12-partition plate.
The technical scheme of the present invention will be described in detail with the
accompanying drawings, but the protection scope of the present invention is not limited
to the embodiments.
Embodiment 1: the invention comprises a cylindrical shell 5, a distillate outlet 4, an upper
circular head 3, a lower circular head 6, a hollow fiber membrane group, a hollow tube
group and a grid screen 11 arranged in the cylindrical shell 5.
The cylindrical shell 5 has a height of 1600 mm, an inner diameter of 60 mm, and a wall
thickness of 5 mm. The cavity in the cylindrical shell 5 is divided into upper, middle and
lower parts. Partition plates 12 are respectively arranged in the upper and lower cavities
to divide them into symmetrical inner cavity structures. The middle cavity communicates
with the inner cavities of the upper and lower cavities. Twenty groups of hollow fiber
membrane groups are arranged in the two inner cavities on different sides of the upper
and lower cavities. Each hollow fiber membrane group consists of polypropylene hollow fiber membranes 9 with an inner diameter of 0.5 mm, a wall thickness of 0.25 mm, a pore diameter of 0.25 [m, a porosity of 0.6 and a length of 1500 mm, wherein the two ends of the hollow fiber membranes 9 are fixed in a single row according to the adjacent spacing of 0.3 mm. Two inner cavities on different sides of the upper cavity and the lower cavity are provided with 20 groups of hollow tube groups, and each group of hollow tube groups consists of polypropylene hollow tubes 10 with an inner diameter of 0.5 mm, a wall thickness of 50 um and a length of 1500 mm, wherein two ends of the hollow tubes 10 are fixed in a single line row according to the adjacent spacing of 0.3 mm. The hollow tube group and the hollow fiber membrane group in the middle cavity are arranged in an
X-shaped cross way. A Grid screen 11 is arranged in the middle cavity to separate the
hollow tube group and the hollow fiber membrane group, so that the hollow tube group
and the hollow fiber membrane group are arranged alternately, the mesh number of the
grid screen 11 is 40 meshes, and the material is polypropylene. The distillate outlet 4 is
arranged on the side wall of the middle cavity, and the absorption liquid inlet 13 is
closed. The upper circular head 3 is connected with the top end of the cylindrical shell 5
through a concave-convex flange, and the lower circular head 6 is connected with the
bottom end of the cylindrical shell 5 through a concave-convex flange. The sealing
performance between the cylindrical shell 5, the upper circular head 3 and the lower
circular head 6 can be effectively improved by the concave-convex flanges. The upper
circular head 3 is provided with a hollow fiber membrane group feed port 8
communicating with hollow fiber membrane groups and a hollow tube group discharge
port 7 communicating with hollow tube groups, while the lower circular head 6 is
provided with a hollow fiber membrane group discharge port 2 communicating with hollow fiber membrane groups and a hollow tube group feed port 1 communicating with hollow tube groups. The effective membrane area of the countercurrent exchange membrane distillation device is 1 in2
. The countercurrent exchange membrane distillation device with the above structure can
be applied to the treatment processes of seawater desalination, reclaimed water reuse and
industrial high salinity wastewater concentration. Taking the desalination process of
industrial high-salinity wastewater (sodium chloride mass concentration is 5%) as an
example, the detailed description is as follows. The saline wastewater to be treated at
normal pressure with a temperature of 20-50°C and a flow rate of 30 L/h enters the
hollow tube groups in the cylindrical shell 5 through the hollow tube group feed port 1 of
the membrane distiller, and performs countercurrent heat exchange with the existing
saline wastewater in the hollow fiber membrane groups, so that the saline wastewater in
the hollow tube groups is preheated. The saline wastewater is output from the hollow tube
group discharge port 7, further raises to 95°C after external supplementary heat exchange,
and enters the hollow fiber membrane groups from the hollow fiber membrane group feed
port 8. In the process of countercurrent heat exchange, the saline wastewater of hollow
fiber membrane groups evaporates continuously, the concentrated wastewater formed by
continuous enrichment of salt concentration flows out from the hollow fiber membrane
group discharge port 2. The water vapor formed after evaporation of saline wastewater
penetrates through the membrane holes of hollow fiber membrane groups and is cooled
by the newly imported saline wastewater of hollow tube groups to obtain cooled fresh
water, which finally flows out from the distillate port 4 and converges. At this point, the
single-stage membrane distillation process is completed, and the distillation treatment of a large number of saline wastewater can be completed by repeating the cycle of the above steps.
Embodiment 2
The structural form of the countercurrent exchange membrane distillation device in
Embodiment 2 is the same as that in Embodiment 1. The cylindrical shell 5 has a height
of 1600 mm, an inner diameter of 100 mm and a wall thickness of 5 mm. The cavity in
the cylindrical shell 5 is divided into upper, middle and lower parts, and the upper and
lower cavities are respectively divided into symmetrical inner cavity structures by
partition plates 12. The middle cavity communicates with the inner cavities of the upper
and lower cavities. Two inner cavities on different sides of the upper cavity and the lower
cavity are provided with 35 groups of hollow fiber membrane groups, and each group of
hollow fiber membrane groups is composed of polypropylene hollow fiber membranes 9
with inner diameter of 0.5 mm, wall thickness of 0.25 mm, pore diameter of 0.25 [m,
porosity of 0.6 and length of 1500 mm, wherein the two ends of the hollow fiber
membranes 9 are fixed in a single row according to the adjacent spacing of 0.3 mm. Two
inner cavities on different sides of the upper cavity and the lower cavity are provided with
groups of hollow tube groups, and each group of hollow tube groups consists of
polypropylene hollow tubes 10 with an inner diameter of 0.5 mm, a wall thickness of 50
um and a length of 1500 mm, wherein the two ends of the hollow tubes 10 are fixed in a
single line row according to the adjacent spacing of 0.3 mm. The hollow tube group and
the hollow fiber membrane group in the middle cavity are arranged in an X-shaped cross
way. A grid screen 11 is arranged in the middle cavity to separate the hollow tube group
and the hollow fiber membrane group, so that the hollow tube group and the hollow fiber membrane group are arranged alternately, the mesh number of the grid screen 11 is 40 meshes, and the material is polypropylene. The absorption liquid inlet 13 is arranged on the upper side wall of the middle cavity, and the distillate outlet 4 is arranged on the lower side wall of the middle cavity. The upper circular head 3 is connected with the top end of the cylindrical shell 5 through concave-convex flanges, and the lower circular head 6 is connected with the bottom end of the cylindrical shell 5 through concave convex flanges. The sealing performance between the cylindrical shell 5, the upper circular head 3 and the lower circular head 6 can be effectively improved by the concave convex flanges. The upper circular head 3 is provided with a hollow fiber membrane group feed port 8 communicating with hollow fiber membrane groups and a hollow tube group discharge port 7 communicating with hollow tube groups, while the lower circular head 6 is provided with a hollow fiber membrane group discharge port 2 communicating with hollow fiber membrane groups and a hollow tube group feed port 1 communicating with hollow tube groups. The effective membrane area of the countercurrent exchange membrane distillation device is 2.5 M 2 .
Taking the treatment process of deamination of gaseous membrane wastewater with the
countercurrent exchange membrane distillation device with the above structure as an
example, the process is as follows. The ammonia-containing wastewater to be treated at
normal pressure with a temperature of 20-50°C and a flow rate of 80 L/h enters the
hollow tube groups in the cylindrical shell 5 through the hollow tube group feed port 1 of
the membrane distiller, and performs countercurrent heat exchange with the existing
ammonia-containing wastewater in the hollow fiber membrane groups, so that the
ammonia-containing wastewater in the hollow tube groups is preheated. The ammonia- containing wastewater is output from the hollow tube group discharge port 7, further raises to 80°C after external supplementary heat exchange, and enters the hollow fiber membrane group from the hollow fiber membrane group feed port 8. Ammonia gas in ammonia-containing wastewater entering the hollow fiber membrane groups evaporates, penetrates through membrane holes on the membrane wall of the hollow fiber membrane, diffuses to the gap in the cylindrical shell, then is absorbed and collected by the absorption liquid added in the shell, and flows out from the distillate outlet. The ammonia-containing wastewater and the newly input ammonia-containing wastewater of the hollow tube groups undergo countercurrent heat exchange for preheating the newly input ammonia-containing wastewater until the single-stage membrane distillation process is completed, and the distillation treatment of a large amount of ammonia containing wastewater can be completed by repeating the cycle of the above steps.
As described above, although the present invention has been shown and described with
reference to specific preferred embodiments, it should not be interpreted as limiting the
present invention itself. Various changes in form and details may be made therein without
departing from the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. A countercurrent exchange membrane distillation device, characterized by comprising
a cylindrical shell, an absorption liquid inlet, a distillate outlet, an upper circular head and
a lower circular head; The cavity in the cylindrical shell is divided into upper, middle and
lower parts, the upper and lower cavities are respectively provided with partition plates to
divide them into symmetrical inner cavity structures, the middle cavity is communicated
with the inner cavities of the upper and lower cavities, at least 5 hollow tube groups are
arranged in two inner cavities on different sides of the upper and lower cavities, and at
least 5 hollow fiber membrane groups are arranged in two inner cavities on different sides
of the upper and lower cavities; A Grid screen is arranged in the middle cavity to separate
the hollow tube group and the hollow fiber membrane group, so that the hollow tube
group and the hollow fiber membrane group are arranged alternately; The absorption
liquid inlet is arranged at the upper part of the side wall of the middle cavity, the distillate
outlet is arranged at the lower part of the side wall of the middle cavity, the upper circular
head is connected with the top end of the cylindrical shell through a concave-convex
flange, and the lower circular head is connected with the bottom end of the cylindrical
shell through a concave-convex flange; The upper circular head is provided with a hollow
fiber membrane group feed port communicating with hollow fiber membrane groups and
a hollow tube group discharge port communicating with hollow fiber membrane groups;
The lower circular head is provided with a hollow fiber membrane group discharge port
communicating with the hollow fiber membrane groups and a hollow tube group feed
port communicating with the hollow tube groups.
2. The countercurrent exchange membrane distillation device according to claim 1,
characterized in that the hollow tube group and the hollow fiber membrane group in the
middle cavity are arranged in an X-shaped cross.
3. The countercurrent exchange membrane distillation device according to claim 2,
characterized in that the hollow fiber membrane group consists of 100-800 hollow fiber
membranes with inner diameter of 0.2-1 mm, wall thickness of 0.2-0.5 mm, pore
diameter of 0.2-0.8um, porosity of 0.4-0.8 and length of 500-1800 mm in diagonal single
row arrangement.
4. The countercurrent exchange membrane distillation device according to claim 2,
characterized in that the hollow tube group consists of 100-800 hollow tubes with an
inner diameter of 0.2-1mm, a wall thickness of 5-100um and a length of 500-1800 mm in
diagonal single row arrangement.
5. The countercurrent exchange membrane distillation device according to claim 2,
characterized in that the mesh number of the grid screen is 10-100.
6. The countercurrent exchange membrane distillation device according to claim 2,
characterized in that the cylindrical shell has a height of 10003000 mm, an inner
diameter of 50-500 mm and a wall thickness of 4-40 mm.
7. The countercurrent exchange membrane distillation device according to claim 2,
characterized in that the heights of the upper circular head and the lower circular head are
both 30 mm.
8. A method for treating saline wastewater by using the countercurrent exchange
membrane distillation device of claim 2, characterized by comprising the following steps:
(1) The saline wastewater to be treated input from the hollow tube group feed port enters
the hollow tube groups, undergoes countercurrent heat exchange with the high
temperature saline wastewater existing in the hollow fiber membrane groups, and then is
output from the hollow tube group discharge port;
(2) The preheated saline wastewater output from the hollow tube group discharge port is
further raised to the vaporization temperature after external supplementary heat exchange,
and enters the hollow fiber membrane groups in the cylindrical shell from the hollow
fiber membrane group feed port;
(3) The saline wastewater enters the hollow fiber membrane groups and the newly input
saline wastewater of the hollow tube groups undergo countercurrent heat exchange, the
heat is released, the water vapor diffuses to the gap in the cylindrical shell through the
membrane holes on the membrane wall of the hollow fiber membrane, and the permeate
is cooled to become liquid, and discharged from the distillate outlet, so that the single
stage membrane distillation process is completed;
(4) Repeat the cycle of steps (1) to (3) to complete the distillation process of a large
amount of saline wastewater.
9. A method for treating ammonia-containing wastewater by using the countercurrent
exchange membrane distillation device of claim 2, characterized by comprising the
following steps:
(1) Ammonia-containing wastewater to be treated input from the hollow tube group feed
port enters the hollow tube group, undergoes countercurrent heat exchange with the high
temperature ammonia-containing wastewater existing in the hollow fiber membrane
groups, and then is output from the hollow tube group discharge port;
(2) The preheated ammonia-containing wastewater output from the hollow tube group
discharge port is further heated by external supplementary heat exchange, and enters the
hollow fiber membrane groups in the cylindrical shell from the hollow fiber membrane
group feed port;
(3) Ammonia in the ammonia-containing wastewater entering the hollow fiber membrane
groups evaporates and diffuses to the gap in the cylindrical shell through the membrane
holes on the hollow fiber membrane wall, and is absorbed and collected by the absorption
liquid added in the shell and flows out from the distillate outlet; At the same time, the
ammonia-containing wastewater and the newly input ammonia-containing wastewater of
the hollow tube groups undergo countercurrent heat exchange for preheating the newly
input ammonia-containing wastewater, so that the single-stage membrane distillation
process is completed; The absorption liquid includes but is not limited to sulfuric acid,
hydrochloric acid and nitric acid;
(4) Repeat the cycle of steps (1) to (3) to complete the distillation treatment process of a
large amount of ammonia-containing wastewater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2021104798A AU2021104798A4 (en) | 2021-08-02 | 2021-08-02 | Countercurrent Exchange Membrane Distillation Device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| AU2021104798A AU2021104798A4 (en) | 2021-08-02 | 2021-08-02 | Countercurrent Exchange Membrane Distillation Device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2021104798A4 true AU2021104798A4 (en) | 2021-09-30 |
Family
ID=77857679
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2021104798A Active AU2021104798A4 (en) | 2021-08-02 | 2021-08-02 | Countercurrent Exchange Membrane Distillation Device |
Country Status (1)
| Country | Link |
|---|---|
| AU (1) | AU2021104798A4 (en) |
-
2021
- 2021-08-02 AU AU2021104798A patent/AU2021104798A4/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100567180C (en) | The treatment process of the epoxy resin waste-water of high alkalinity, high salt, high organic content | |
| CN106045035B (en) | A kind of ternary sewage water treatment method for coupling anaerobic acid-production, positive infiltration and microbiological fuel cell | |
| CN101475280B (en) | Zero discharge wastewater treatment method, liquid membrane crystal wastewater evaporator and application system | |
| CN203990317U (en) | The stifled energy-saving film distiller of a kind of normal pressure anti-soil | |
| CN101147845A (en) | Hollow fiber pressure reducing film distillation film component device and method | |
| AU2021104798A4 (en) | Countercurrent Exchange Membrane Distillation Device | |
| CN202046964U (en) | High-efficiency sewage treating device | |
| CN203990316U (en) | A kind of counterflow exchange distillation device | |
| CN211497025U (en) | Forward osmosis and combined soda production process co-production combined system | |
| CN204454816U (en) | The treatment system of nitrogen-containing wastewater | |
| CN212924700U (en) | Recycling process system for treating nitrogen and phosphorus-containing wastewater | |
| CN204625433U (en) | The reactor of a kind of chemical-biological combined removal nitre nitrogen and ammonia nitrogen | |
| CN211226764U (en) | Retrieve device of copper in follow copper-containing waste liquid | |
| CN203155102U (en) | Membrane distiller | |
| CN212640167U (en) | Membrane diffusion coagulation pretreatment system | |
| CN212924701U (en) | Membrane distillation reverse osmosis two-stage membrane crystallization wastewater treatment system | |
| CN110577325B (en) | Processing system of high salt high organic matter waste water resourceization and zero release | |
| CN210729178U (en) | Double-sided cooling multi-runner membrane distillation device | |
| CN103466872A (en) | Wastewater treatment method for producing hydrogenation catalyst of heavy oil | |
| CN203007082U (en) | Countercurrent multiple-effect evaporation device | |
| CN203284286U (en) | Sewage recycling and zero-emission device for coal chemical industry | |
| CN102190399A (en) | Method for electrochemically regenerating zeolite subjected to anerobic biochemical treatment and ammonia nitrogen adsorption | |
| CN104147932A (en) | Normal-pressure pollution and plugging resistant energy-saving membrane distiller | |
| CN213652119U (en) | Immersion reaction assembly and recovery system for recovering nitrogen in wastewater with high ammonia nitrogen content | |
| CN110790441A (en) | Device and method for recovering copper from copper-containing waste liquid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FGI | Letters patent sealed or granted (innovation patent) |