CN106861353A - Separating device - Google Patents
Separating device Download PDFInfo
- Publication number
- CN106861353A CN106861353A CN201510960790.2A CN201510960790A CN106861353A CN 106861353 A CN106861353 A CN 106861353A CN 201510960790 A CN201510960790 A CN 201510960790A CN 106861353 A CN106861353 A CN 106861353A
- Authority
- CN
- China
- Prior art keywords
- space
- pump
- boiling point
- tower
- destilling tower
- 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
- 238000009835 boiling Methods 0.000 claims abstract description 117
- 239000007788 liquid Substances 0.000 claims abstract description 61
- 239000000126 substance Substances 0.000 claims abstract description 38
- 239000000463 material Substances 0.000 claims description 71
- 239000002912 waste gas Substances 0.000 claims description 38
- 239000012141 concentrate Substances 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 11
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 238000004821 distillation Methods 0.000 abstract 2
- 230000001105 regulatory effect Effects 0.000 description 15
- 238000010586 diagram Methods 0.000 description 14
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 12
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 10
- 239000007789 gas Substances 0.000 description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 230000000052 comparative effect Effects 0.000 description 8
- 230000005540 biological transmission Effects 0.000 description 7
- 239000012530 fluid Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000002904 solvent Substances 0.000 description 7
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical class CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 5
- 239000012855 volatile organic compound Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000004814 polyurethane Substances 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 3
- 229910021645 metal ion Inorganic materials 0.000 description 3
- 239000011859 microparticle Substances 0.000 description 3
- LLHKCFNBLRBOGN-UHFFFAOYSA-N propylene glycol methyl ether acetate Chemical compound COCC(C)OC(C)=O LLHKCFNBLRBOGN-UHFFFAOYSA-N 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 238000010025 steaming Methods 0.000 description 3
- DAFHKNAQFPVRKR-UHFFFAOYSA-N (3-hydroxy-2,2,4-trimethylpentyl) 2-methylpropanoate Chemical compound CC(C)C(O)C(C)(C)COC(=O)C(C)C DAFHKNAQFPVRKR-UHFFFAOYSA-N 0.000 description 2
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- WUOACPNHFRMFPN-UHFFFAOYSA-N alpha-terpineol Chemical compound CC1=CCC(C(C)(C)O)CC1 WUOACPNHFRMFPN-UHFFFAOYSA-N 0.000 description 2
- SQIFACVGCPWBQZ-UHFFFAOYSA-N delta-terpineol Natural products CC(C)(O)C1CCC(=C)CC1 SQIFACVGCPWBQZ-UHFFFAOYSA-N 0.000 description 2
- 229940028356 diethylene glycol monobutyl ether Drugs 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- JCGNDDUYTRNOFT-UHFFFAOYSA-N oxolane-2,4-dione Chemical compound O=C1COC(=O)C1 JCGNDDUYTRNOFT-UHFFFAOYSA-N 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229940116411 terpineol Drugs 0.000 description 2
- -1 triethylene glycol, propane diols Chemical class 0.000 description 2
- ZAZVCYBIABTSJR-UHFFFAOYSA-N (+)-Abienol Natural products CC1(C)CCCC2(C)C(CC=C(C=C)C)C(C)(O)CCC21 ZAZVCYBIABTSJR-UHFFFAOYSA-N 0.000 description 1
- ZAZVCYBIABTSJR-KOQQBVACSA-N Abienol Chemical compound CC1(C)CCC[C@]2(C)C(CC=C(C=C)C)[C@](C)(O)CC[C@H]21 ZAZVCYBIABTSJR-KOQQBVACSA-N 0.000 description 1
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 1
- 229920002334 Spandex Polymers 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- YBCVMFKXIKNREZ-UHFFFAOYSA-N acoh acetic acid Chemical compound CC(O)=O.CC(O)=O YBCVMFKXIKNREZ-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical class OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 1
- 125000000484 butyl group Chemical group [H]C([*])([H])C([H])([H])C([H])([H])C([H])([H])[H] 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- KKTBXRFTXPLJNN-UHFFFAOYSA-N ent-labd-8beta-ol-14-ene Natural products CC(CCC1C(C)(O)CCC2C(C)(C)CCCC12C)C=C KKTBXRFTXPLJNN-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- WFKAJVHLWXSISD-UHFFFAOYSA-N isobutyramide Chemical compound CC(C)C(N)=O WFKAJVHLWXSISD-UHFFFAOYSA-N 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910001416 lithium ion Inorganic materials 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
- 229920006254 polymer film Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000004759 spandex Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- RBNWAMSGVWEHFP-UHFFFAOYSA-N trans-p-Menthane-1,8-diol Chemical compound CC(C)(O)C1CCC(C)(O)CC1 RBNWAMSGVWEHFP-UHFFFAOYSA-N 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
- B01D53/002—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 condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/141—Fractional distillation or use of a fractionation or rectification column where at least one distillation column contains at least one dividing wall
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/42—Regulation; Control
- B01D3/4211—Regulation; Control of columns
- B01D3/4216—Head stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention discloses a separation device which comprises a dividing wall type distillation tower, a first heater, a second heater, a first pump, a first condenser, a second pump, a third pump, a fifth pump and a second condenser. The dividing wall distillation column includes a packed bed, an inlet, a first space, a second space, and a third space. An inlet is connected to the first space and located below the packed bed and is configured to receive the mixed liquid. The mixed liquid contains high boiling point substances, medium boiling point substances and low boiling point substances. The first pump pumps out the middle boiling point substance in the vapor state in the second space. The first condenser condenses the extracted medium boiling point substances. The second pump pumps the high boiling point substance in the liquid state in the first space. The third pump pumps the liquid medium boiling point substance and part of the high boiling point substance in the second space. The second condenser condenses the low boiling point substance in a vapor state discharged from the third space. And the fifth pump pumps out the condensed low boiling point substances in liquid state.
Description
Technical field
The present invention relates to a kind of separator, and more particularly to a kind of separation that may separate out various boilers
Device.
Background technology
VOC (Volatile Organic Compounds, VOCs) waste gas is usually contained perhaps
The different organic solvent of multicomponent.Current industry treatment VOCs is condensed nothing more than absorption, directly, or combustion
The modes such as burning.However, this solvent recovering rate obtained by a little modes is relatively low and relatively costly.
Therefore, need badly and propose a kind of technology of new solvent-recoverable.
The content of the invention
It is an object of the invention to provide it is a kind of can be by the technology of recycling design in volatile organic waste gas.According to
One embodiment of the invention, proposes a kind of separator.Separator includes a bulkhead type destilling tower, one the
One heater, a secondary heater, one first pump, one first condenser, one second pump, one the 3rd pump,
One the 5th pump and one second condenser.Bulkhead type destilling tower, including a packed bed, a first entrance and one point
Dividing plate, it is empty that the inside of bulkhead type destilling tower is distinguished into one first space, a second space and the 3rd by demarcation strip
Between, first entrance connects the first space and positioned at the lower section of packed bed and is used to receive a mixing liquid, mixes
Liquid includes a high boiling substance, a mid boiling point materials and a low boilers.Primary heater provide heat to
First space.Secondary heater provides heat to second space.First pump is connected to bulkhead type destilling tower and use
To extract the mid boiling point materials in steam state in second space out.First condenser is connected to the first pump, and is used to
Condense by the mid boiling point materials of the first pumped.Second pump is connected to one first bottom in the first space, to take out
The high boiling substance being in a liquid state gone out in the first space.3rd pump is connected to one second bottom of second space,
To extract the mid boiling point materials being in a liquid state in second space and part high boiling substance out.Second condenser connects
It is connected to bulkhead type destilling tower and is used to condense the low-boiling point material in steam state from the discharge of the 3rd space, the 5th pump
The second condenser is connected to, and is used to extract the condensed low-boiling point material being in a liquid state of the second condenser out.
According to another embodiment of the present invention, propose that a kind of separator includes that a first entrance, one first steam
Evaporate tower, an after-fractionating tower), it is a primary heater, a secondary heater, one first pump, one first cold
Condenser, one second pump, one the 3rd pump, one the 4th pump, one second condenser, one first accumulator tank and 1
Five pumps.First destilling tower, including a second entrance, second entrance are used to receive a waste gas, and waste gas includes one
High boiling substance, a mid boiling point materials and a low-boiling point material.Primary heater provides heat to after-fractionating
First space of tower, secondary heater provides second space of the heat to after-fractionating tower.First pump is connected to
After-fractionating tower, and it is used to extract out the mid boiling point materials in steam state in after-fractionating tower.First condenser is used
To condense by the mid boiling point materials of the first pumped.Second pump is connected to the first bottom of after-fractionating tower, with
Extract the high boiling substance being in a liquid state in the first bottom out.3rd pump is connected to the second bottom of after-fractionating tower
Portion, to extract the mid boiling point materials being in a liquid state in the second bottom and part high boiling substance out.4th pump connects
The first destilling tower and after-fractionating tower are connect, and is used to extract out the concentration of the waste gas in the bottom of the first destilling tower
Liquid, and it is delivered to the first entrance of after-fractionating tower.Second condenser connect the first destilling tower, and be used to by
From the waste gas condensation of the one of the first destilling tower top discharge into a storing liquid.First accumulator tank is used to storage
Liquid.5th pump connects the first destilling tower and the first accumulator tank, and is used to take out storing liquid from the first accumulator tank
Go out and be delivered to the top of the first destilling tower.
Below in conjunction with the drawings and specific embodiments, the present invention will be described in detail, but not as to of the invention
Limit.
Brief description of the drawings
Fig. 1 illustrates the schematic diagram according to the separator of one embodiment of the invention；
Fig. 2 illustrates the schematic diagram according to the separator of another embodiment of the present invention；
Fig. 3 illustrates the schematic diagram according to the separator of another embodiment of the present invention；
Fig. 4 illustrates the schematic diagram according to the separator of another embodiment of the present invention；
Fig. 5 illustrates the schematic diagram according to the separator of another embodiment of the present invention；
Fig. 6 illustrates the schematic diagram according to the separator of another embodiment of the present invention；
Fig. 7 illustrates the schematic diagram according to the separator of another embodiment of the present invention.
Wherein, reference
100、200、300、400、500、600、700：Separator
110：Bulkhead type destilling tower or after-fractionating tower
111：Packed bed
110a1：First entrance
112：Demarcation strip
113、212：Top
120：Primary heater
125：First pump
130：Second pump
135：First condenser
140：Second condenser
145：5th pump
150：Secondary heater
160：3rd pump
210：First destilling tower
210a：Second entrance
211：Bottom
220：4th pump
230：First accumulator tank
250：First regulating valve
260：Second regulating valve
270：Connecting line
510：3rd condenser
520：Second accumulator tank
530：6th pump
a’：Entrance
G1：High-temp waste gas
G2：Low temperature waste gas
G3：Purification waste gas
g1：High boiling substance
g2：Mid boiling point materials
g21：Mid-boiling point liquid
g22：Mid-boiling point gas
g3：Low-boiling point material
L1：Concentrate
L2：Storing liquid
L3：Mixing liquid
P1：First space
P11：First bottom
P2：Second space
P21：Second bottom
P3：3rd space
Specific embodiment
Structural principle of the invention and operation principle are described in detail below in conjunction with the accompanying drawings：
Fig. 1 is illustrated according to the schematic diagram of separator 100 of one embodiment of the invention.Separator 100 is for example
It is a liquid treatment equipment.
Separator 100 includes bulkhead type destilling tower 110, primary heater 120, the first pump 125, the
Two pumps 130, the first condenser 135, the second condenser 140, secondary heater 150, the 3rd pump 160
And the 5th pump 145.This little element therebetween can be connected by entity pipeline, with the fluid between transmission.
Bulkhead type destilling tower 110 includes at least a packed bed 111, first entrance 110a1 and demarcation strip 112.
The inside of bulkhead type destilling tower 110 is distinguished into the first space P1, second space P2 and by demarcation strip 112
Three space P3, wherein the first space P1 and second space P2 is located at the bottom of bulkhead type destilling tower 110,
And the 3rd space P3 is located at the top of bulkhead type destilling tower 110.
First entrance 110a1 connects the first space P1 and is used to receive a mixing liquid L3, such as blended liquid phase
Logistics.First entrance 110a1 is located at the lower section of packed bed 111.It is located at compared to first entrance 110a1
The top of packed bed 111, because the first entrance 110a1 of the present embodiment is located at the lower section of packed bed 111,
Therefore can avoid containing easy polymeric material or microparticle impurity obstruction packed bed 111 in mixing liquid L3.
Further say, when packed bed 111 is porous material, due to the first entrance 110a1 of the present embodiment
Positioned at the lower section of packed bed 111, therefore can avoid containing easy polymeric material or micro- in mixing liquid L3
The hole of grain obstruction packed bed 111.
By the separator 100 of the embodiment of the present invention, can be by organic volatile in mixing liquid L3 not
It is individually separated out with the composition of boiling point.How will be described below by organic volatile in mixing liquid L3
The composition of different boiling is individually separated out.In the present embodiment, mixing liquid L3 is, for example, comprising various
The material of different boiling, such as high boiling substance g1, mid boiling point materials g2 and low-boiling point material g3.
Primary heater 120 can provide heat to the first space P1.For example, primary heater 120 from point
Heat is provided at the lower section of the packed bed 111 of wall type destilling tower 110 to the first space P1.Second pump 130
The first bottom P11 of the first space P1 is connected, to extract the height boiling being in a liquid state in the first space P1 out
Point material g1.
Additionally, the heating-up temperature of primary heater 120 can be higher than the boiling point of mid boiling point materials g2, make middle boiling
Point material g2 and low-boiling point material g3 can flash to steam state, and be up distributed in the first space of part P1,
Second space P2 and the 3rd space P3.Can be from bulkhead type destilling tower 110 in the low-boiling point material g3 of steam state
Top 113 discharge outward.Second condenser 140 it is condensable from the 3rd space P3 discharges in steam state
Low-boiling point material g3.
Secondary heater 150 can provide heat and give second space P2, to ensure that low-boiling point material g3 is protected
Hold steam state and toward up to the 3rd space P3, finally discharged outward from the top 113 of bulkhead type destilling tower 110.
The second bottom P21 of the connection second space of the 3rd pump 160 P2, in extracting out in second space P2
Boilers g2 and part high boiling substance g1.During first pump 125 can be extracted out in second space P2
Boiling point gas g22, and the mid-boiling point gas g22 after the condensable extraction of the first condenser 135.It is condensed
The recyclable recyclings of mid-boiling point gas g22.Further say, when mixing liquid L3 contains metal ion,
Metal ion usually there will be in liquid, and be not present in gas, therefore condensed mid-boiling point gas g22
It is recyclable to be reused in the industry higher for metal ion specification requirement.In one embodiment, mid-boiling point vapour
The purity of body g22 can be higher than 99.5wt%.
Fig. 2 is illustrated according to the schematic diagram of separator 200 of another embodiment of the present invention.Separator 200
E.g. waste gas treatment equipment, it can process high-temp waste gas, and reclaim the organic solvent in waste gas.
Separator 200 include the first destilling tower 210, first entrance 110a1, primary heater 120,
Secondary heater 150, the second pump 130, the second condenser 140, the 3rd pump 160, after-fractionating tower 110,
4th pump 220, the first accumulator tank 230, the 5th pump 145, the first regulating valve 250, the second regulating valve 260
And connecting line 270, after-fractionating tower therein is, for example, above-mentioned bulkhead type destilling tower 110.Additionally, this
A little elements can be connected therebetween by entity pipeline, with the fluid between transmission.
First destilling tower 210 includes second entrance 210a, the acceptable high-temp waste gas G1 of second entrance 210a.
High-temp waste gas G1 is, for example, VOCs.In one embodiment, high-temp waste gas G1 can include various differences
The material of boiling point, such as high boiling substance g1, mid boiling point materials g2 and low-boiling point material g3.In an embodiment
In, high boiling substance g1 and mid boiling point materials g2 are, for example, organic volatile, and low-boiling point material g3
Air in this way.In one embodiment, high-temp waste gas G1 comprising organic volatile (such as high boiling substance g1 and in
Boilers g2), wherein organic volatile is, for example, to be selected from by dimethylacetylamide, acetic acid, N- methyl
Pyrrolidones (N-Methyl-2-pyrrolidone), dimethylformamide, propylene glycol methyl ether acetate
(Propylene Glycol Mono-methyl Ether Acetate, PGMEA), dimethyl sulfoxide (DMSO), second
Glycol, diethylene glycol, triethylene glycol, propane diols, 1,4- butanediols, diethylene glycol monobutyl ether
(diethylene glycol monobutyl ether；BDG), monoethanolamine (Monoethanolamine),
The group that abienol (Terpineol) and alcohol ester 12 (Texanol) are constituted.
In some techniques, such as polymer film (Polyimide Film) technique, lithium-ion electric pool process, bullet
Property fiber (Spandex) technique and polyurethane (Polyurethane, PU) skin technique, its waste gas for being discharged
Usually contain the solvent that higher boiling, burning tend to have NOx and unit price high, such as 1-METHYLPYRROLIDONE (NMP),
Dimethylformamide (DMAc) and/or dimethylformamide (DMF).By the separator of the embodiment of the present invention
200 can fully reclaim this little unit price solvent high, and purify the waste gas of externally discharge.Additionally, by this hair
The separator 200 of bright embodiment, also can fully reclaim other solvents, such as acetic acid (Acetic acid),
Terpinol (Terpineol), Texanol, butyl (DBG), dimethyl sulfoxide (DMSO) (DMSO) and/
Or MEA (MEA).For application field, the separator 200 of the embodiment of the present invention can be applied to
Semiconductor, photoelectric panel, solar energy, fuel cell industry, organic film, fiber industry, PU synthesis skins
Deng field.
After high-temp waste gas G1 enters the first destilling tower 210, in the Nei With Come of the first destilling tower 210 from the first storage
The low Warm storing liquids L2 for depositing groove 230 carries out gas-liquid contact, high boiling substance g1 contained by part waste gas G1,
After mid boiling point materials g2 and a small amount of low-boiling point material g3 are condensed into concentrate L1, flow down to first steams
Evaporate the bottom 211 of tower 210, and low-boiling point material g3 With of the waste gas that another part is not condensed contained by it
A small amount of high boiling substance g1, a small amount of mid boiling point materials g2 forms Di Warm Waste Gas G2.Low temperature waste gas G2
Up flow to the top 212 of the first destilling tower 210 and flow to the second condenser 140 outward.
For for positioned at the processing mode of the concentrate L1 of the bottom 211 of the first destilling tower 210, the
Four pumps 220 can extract the concentrate L1 in the bottom 211 of the first destilling tower 210 out and export to bulkhead type and steam
Tower 110 is evaporated, allows bulkhead type destilling tower 110 to isolate the material of different boiling.
Concentrate L1 can enter inside bulkhead type destilling tower 110 from first entrance 110a1.Concentrate L1
Temperature be, for example, between 30 degree to 250 degree Celsius.In the present embodiment, first entrance 110a1
Connect the first space P1 and be configured at the top of packed bed 111, be so also configured in filling out in another embodiment
Fill the lower section of bed 111.
After concentrate L1 enters the inside of bulkhead type destilling tower 110, due to the heating temperature of primary heater 120
Boiling point of the degree higher than mid boiling point materials g2, makes the mid boiling point materials g2 of concentrate L1 and low-boiling point material g3
Steam state is flashed to, and is distributed in the first space of part P1, second space P2 and the 3rd space P3.Due to
The heating-up temperature of one heater 120 is less than high boiling substance g1, makes high boiling substance g1 flow downs to the
The first bottom P11 of one space P1.Second pump 130 can extract the high boiling substance g1 being in a liquid state out.As schemed
Shown in 2, the high boiling substance g1 being in a liquid state extracted out by the second pump 130 can be discharged partly, and another portion
After lease making crosses the heating of primary heater 120, then it is fed back in bulkhead type destilling tower 110.
As shown in Fig. 2 being distributed in the interior mid boiling point materials g2 partial condensations in steam state of second space P2 into liquid
State down accumulates on the second bottom P21 of second space P2, and is extracted out from bulkhead type steaming by the 3rd pump 160
Evaporate outside tower 110.
Secondary heater 150 can provide heat and give second space P2, to ensure that low-boiling point material g3 is protected
Hold steam state and toward up to the 3rd space P3, finally discharged outward from the top 113 of bulkhead type destilling tower 110.
The low-boiling point material g3 being distributed in the 3rd space P3 in steam state can be from the top of bulkhead type destilling tower 110
113 are expelled to the second condenser 140, and after being condensed into storing liquid L2 by the second condenser 140, are stored in
In first accumulator tank 230.
Just given up for the low temperature for flowing to the second condenser 140 outward from the top 212 of the first destilling tower 210
For the processing mode of gas G2, the condensable top 212 from the first destilling tower 210 of the second condenser 140
The low temperature waste gas G2, low-boiling point material g3 With contained in condensed low temperature waste gas G2 of discharge are a small amount of
High boiling substance g1, a small amount of mid boiling point materials g2 be transformed into liquid (hereinafter referred to as storing liquid L2) and store up
It is stored in the first accumulator tank 230.Due to organic volatile, e.g. high boiling substance g1 and mid boiling point materials
G2 has been completely dissolved in storing liquid L2, therefore the gas discharged from the second condenser 140 (hereinafter referred to as purifies waste gas
G3 organic volatile concentration) is very low.In one embodiment, the organic volatile concentration of purification waste gas G3 can
Less than 30ppm, even less than 1ppm.In summary, the first destilling tower 210 of the embodiment of the present invention
Can reach the effect of purification waste gas.
Storing liquid L2 can be extracted out from the first accumulator tank 230 and is delivered to bulkhead type destilling tower by the 5th pump 145
In 110 top 113.After storing liquid L2 enters top 113, it is possible to decrease the temperature of the 3rd space P3,
Avoid the temperature of the 3rd space P3 too high；Further say, storing liquid L2 has regulation bulkhead type destilling tower
Technology effect of 110 internal temperatures.
Additionally, the first regulating valve 250 is configured at the pipeline between the 5th pump 145 and bulkhead type destilling tower 110,
The flow of the controllable storing liquid L2 entered in top 113, with more accurately regulation bulkhead type destilling tower 110
The temperature of interior 3rd space P3.
Additionally, can be delivered to storing liquid L2 in the top 212 of the first destilling tower 210 by the 5th pump 145,
To wash the low high-temp waste gas G1 in the first destilling tower 210, by the organic volatile band in high-temp waste gas G1
The concentrate L1 of high concentration organic volatile material is formed to the bottom 211 of the first destilling tower 210, and can be dropped
The organic volatile concentration of the low temperature waste gas G2 that the low top 212 from the first destilling tower 210 is discharged, maintains
The storing liquid L2 of low concentration organic volatile material, and reach the purpose for separating organic volatile in waste gas.Separately
Outward, the second regulating valve 260 is configured at , Ke Tone on the pipeline between the 5th pump 145 and the first destilling tower 210
The flow of the storing liquid L2 that Festival enters in the top 212 of the first destilling tower 210, to control low temperature waste gas G2
The content of middle organic volatile material.
Connecting line 270 can connect the 5th pump 145 and the first accumulator tank 230, to balance the 5th pump 145
Pump-out and water yield.In the present embodiment, a regulating valve (not illustrating) is optionally installed in connecting tube
On road 270, with the flow of controlling transmission.
Fig. 3 is illustrated according to the schematic diagram of separator 300 of another embodiment of the present invention.Separator 300
Including the first destilling tower 210, first entrance 110a1, primary heater 120, secondary heater 150,
Two pumps 130, the second condenser 140, the 3rd pump 160, after-fractionating tower, the 4th pump 220, first are stored
Groove 230, the 5th pump 145, the first regulating valve 250, the second regulating valve 260 and connecting line 270, wherein
After-fractionating tower be, for example, above-mentioned bulkhead type destilling tower 110.Additionally, this little element therebetween can be by
Entity pipeline is connected, with the fluid between transmission.
Secondary heater 150 can provide heat and give second space P2, to ensure that low-boiling point material g3 is protected
Hold steam state and toward up to the 3rd space P3, finally discharged outward from the top 113 of bulkhead type destilling tower 110.
From unlike the separator 200 of Fig. 2, in the separator 300 of the present embodiment, by the 4th pump
The 220 concentrate L1 for extracting out can be provided to bulkhead type from the lower section of packed bed 111 of bulkhead type destilling tower 110
Inside destilling tower 110.In another embodiment, the concentrate L1 extracted out by the 4th pump 220 can be via first
There is provided again to bulkhead type destilling tower 110 after heater 120；For example, by the 4th pump 220 extract out it is dense
Contracting liquid L1 can enter from the entrance a ' between the second pump 130 and primary heater 120, consequently, it is possible to dense
Contracting liquid L1 can be pushed to primary heater 120 by the second pump 130.
Fig. 4 is illustrated according to the schematic diagram of separator 400 of another embodiment of the present invention.Separator 400
Including the first destilling tower 210, first entrance 110a1, primary heater 120, the first pump 125, the second pump
130th, the first condenser 135, the second condenser 140, secondary heater 150, the 3rd pump 160, second
Destilling tower, the 4th pump 220, the first accumulator tank 230, the 5th pump 145, the first regulating valve 250, second are adjusted
Section valve 260 and connecting line 270, after-fractionating tower therein is, for example, above-mentioned bulkhead type destilling tower 110.
Additionally, this little element therebetween can be connected by entity pipeline, with the fluid between transmission.
Secondary heater 150 can provide heat and give second space P2, to ensure that low-boiling point material g3 is protected
Hold steam state and toward up to the 3rd space P3, finally discharged outward from the top 113 of bulkhead type destilling tower 110.
From unlike the separator 200 of Fig. 2, the separator 400 of the present embodiment further includes the first pump
125 and first condenser 135.First pump 125 and the first condenser 135 of the present embodiment are respectively at
The effect of first pump 125 and the first condenser 135 of the separator 100 of 1 figure is similar to, and holds this and no longer goes to live in the household of one's in-laws on getting married
State.
From unlike the separator 200 of Fig. 2, mid boiling point materials g2 and portion in second space P2
After dividing high boiling substance g1 to be extracted out by the 3rd pump 160, partly bulkhead type is returned to via secondary heater 150
Second space P2, another part of destilling tower 110 distill via bulkhead type is returned to after primary heater 120
First space P1 of tower 110, and other parts are expelled directly out.In another embodiment, second space P2
After interior mid boiling point materials g2 and part high boiling substance g1 is extracted out by the 3rd pump 160, partly via
The second space P2 of bulkhead type destilling tower 110 is returned to after two heaters 150, and remainder is via first
The first space P1 of bulkhead type destilling tower 110 is returned to after heater 120.The embodiment of the present invention is not limited
The processing mode of the mid boiling point materials g2 that is extracted and part high boiling substance g1, is extracted out by the 3rd pump 160
Mid boiling point materials g2 and part high boiling substance g1 can be (1) return to point via secondary heater 150
The second space P2 of wall type destilling tower 110, (2) after primary heater 120 via returning to bulkhead type destilling tower
110 the first space P1 and (3) be discharged directly to separator 200 it is outer at least one situation.
Fig. 5 is illustrated according to the schematic diagram of separator 500 of another embodiment of the present invention.Separator 500
Including the first destilling tower 210, first entrance 110a1, primary heater 120, secondary heater 150,
Two pumps 130, the second condenser 140, the 3rd pump 160, after-fractionating tower, the 4th pump 220, first are stored
Groove 230, the 5th pump 145, the first regulating valve 250, the second regulating valve 260, an at least connecting line 270,
3rd condenser 510, the second accumulator tank 520 and the 6th pump 530, on after-fractionating tower therein is, for example,
State bulkhead type destilling tower 110.Additionally, this little element therebetween can be connected by entity pipeline, to transmit
Between fluid.
From unlike the separator 200 of Fig. 2, it is cold that the separator 500 of the present embodiment further includes the 3rd
Condenser 510, the second accumulator tank 520 and the 6th pump 530.
Further say, the 3rd condenser 510 is condensable to discharge from the top 113 of bulkhead type destilling tower 110
Low-boiling point material g3, condensed low-boiling point material g3 in steam state can be stored in the second accumulator tank 520.
5th pump 145 connects the first accumulator tank 230 and the second accumulator tank 520, in this way, the 5th pump 145 is by first
After storing liquid L2 in accumulator tank 230 is extracted out, the first destilling tower 210 is partly delivered to, and remainder
Second accumulator tank 520 is delivered to by connecting line 270.Storing liquid L2 in second accumulator tank 520 by
After 6th pump 530 is extracted out, partly it is delivered to the top 113 of bulkhead type destilling tower 110 to reconcile bulkhead type steaming
The temperature at the top 113 of tower 110 is evaporated, and remainder can be delivered to the first storage by connecting line 270
Groove 230.
The separator 500 of the present embodiment uses two condensers (the second condenser 140 and the 3rd condensers
510) workload of the single condenser (the second condenser 140) of the separator 200 of contribution graph 2, because
This can mitigate the work load of single condenser；Similarly, the separator 500 of the present embodiment uses two
Accumulator tank (the first accumulator tank 230 and the second accumulator tank 520), therefore the first storage of smaller volume may be selected
The accumulator tank 520 of groove 230 and second, it is to avoid the volume problems of too of single accumulator tank；Similarly, this implementation
The separator 500 of example is using two separators of pump (the 5th pump 145 and the 6th pump 530) contribution graph 2
The workload of 200 single pump (the 5th pump 145), therefore the work load of single pump can be mitigated.
Additionally, when if the first destilling tower 210 is close with the pressure of bulkhead type destilling tower 110, can be cold by second
The condenser 510 of condenser 140 and the 3rd is integrated into single condenser, stores the first accumulator tank 230 and second
Groove 520 is integrated into single accumulator tank and the 5th pump 145 and the 6th pump 530 is integrated into single pump, after integration
Structure be same as or similar to shown in Fig. 2.
Fig. 6 is illustrated according to the schematic diagram of separator 600 of another embodiment of the present invention.Separator 600
Including the first destilling tower 210, first entrance 110a1, primary heater 120, secondary heater 150,
Two pumps 130, the second condenser 140, the 3rd pump 160, after-fractionating tower, the 4th pump 220, first are stored
Groove 230, the 5th pump 145, the first regulating valve 250, the second regulating valve 260, connecting line the 270, the 3rd
Condenser 510, the second accumulator tank 520 and the 6th pump 530, after-fractionating tower therein is, for example, above-mentioned point
Wall type destilling tower 110.Additionally, this little element therebetween can be connected by entity pipeline, between transmission
Fluid.
From unlike the separator 500 of Fig. 5, the concentrate L1 of the separator 600 of the present embodiment
Can enter inside bulkhead type destilling tower 110 from the lower section of packed bed 111, can so avoid concentrate L1 past
Lower obstruction packed bed 111.Further say, in general concentrate L1 contains microparticle；So due to
The first entrance 110a1 of the present embodiment is located at the lower section of packed bed 111, therefore can avoid concentrate L1's
Microparticle blocks the hole of packed bed 111.In another embodiment, concentrate L1 can be from primary heater
120 and the second entrance a ' between pump 130 enters inside bulkhead type destilling tower 110.
Fig. 7 is illustrated according to the schematic diagram of separator 700 of another embodiment of the present invention.Separator 700
Including the first destilling tower 210, first entrance 110a1, primary heater 120, the first pump 125, the second pump
130th, the condenser 140 of the first condenser 135 second, secondary heater 150, the 3rd pump 160, second steam
Tower, the 4th pump 220, the first accumulator tank 230, the 5th pump 145, the first regulating valve 250, second is evaporated to adjust
Valve 260, connecting line 270, the 3rd condenser 510, the second accumulator tank 520 and the 6th pump 530, wherein
After-fractionating tower be, for example, above-mentioned bulkhead type destilling tower 110.Additionally, this little element therebetween can be by
Entity pipeline is connected, with the fluid between transmission.
From unlike the separator 500 of Fig. 5, the separator 700 of the present embodiment further includes the first pump
125 and first condenser 135.First pump 125 and the first condenser 135 of the present embodiment respectively with Fig. 5
Separator 500 the first pump 125, the first condenser 135 effect be similar to, hold this and repeat no more.
As shown in table 1 below and 2, the data of experimental example A and B in table are the separation dresses of the embodiment of the present invention
The software analogue data put, and the software analogue data of the traditional separator of the data system of comparative example C and D.
Additionally, experimental example A and comparative example C be ambient temperature be 36 degree Celsius and ambient humidity be 80% ring
Tested under border, and it in ambient temperature is 10 degree Celsius and ambient humidity that experimental example B and Comparative Example D are
To be tested in the environment of 65%.
As shown in Table 1, the organic volatile concentration of the purification waste gas G3 of experimental example A and B is less than 1ppm,
It is enough to meet blowdown regulation.As shown in Table 2, due to experimental example A and B waste water can fully recycling,
Therefore without wastewater treatment capacity (wastewater zero discharge)；Reviewing comparative example C and D can all produce certain wastewater treatment
Amount, causes cost for wastewater treatment increase, the load increase of sewage treatment equipment and/or this little waste water because nothing
Method is recycled and causes the waste of water resource；Especially in the environment of high-temperature high-humidity, as shown in comparative example C,
Its wastewater treatment capacity is up to 554 kgs/hour.
Table 1
Table 2
Additionally, under low temperature and low humidity degree environment, it usually needs from extraneous amount of makeup water to destilling tower, right this hair
Rate of water make-up of the rate of water make-up of bright embodiment less than conventional column.For example, as shown in table 2, in low temperature and low humidity
Under degree environment, the rate of water make-up (such as 94 kgs/hour) of experimental example B compared to Comparative Example D (such as 107 kilograms/
Hour) rate of water make-up it is less, can so conserve water cost.In addition, as shown in Table 2, working solvent is (e.g.,
Mid-boiling point gas g22) the rate of recovery may be up to 97.8%, and be not less than traditional separator.
In summary, the separator of the embodiment of the present invention has the existing advantage of comparative example C and D, and volume
Outer to have the advantages that comparative example C and D lack, such as rate of water make-up is few, Sewage treatment is recycled, wastewater discharge
Less or wastewater zero discharge, the rate of recovery of working solvent it is high, it is the working solvent that reclaims that purity is high and/or waste gas
The advantages of effectively purifying.Further, since the condenser of the embodiment of the present invention, pump, accumulator tank can allow two steamings
Evaporating tower to be used in conjunction with, therefore build the cost of whole separator can also be greatly reduced.
Certainly, the present invention can also have other various embodiments, in the feelings without departing substantially from spirit of the invention and its essence
Under condition, those of ordinary skill in the art work as can make various corresponding changes and deformation according to the present invention, but
These corresponding changes and deformation should all belong to the protection domain of appended claims of the invention.
Claims (14)
1. a kind of separator, it is characterised in that including：
One bulkhead type destilling tower, including a packed bed, a first entrance and a demarcation strip, the demarcation strip should
The inside of bulkhead type destilling tower is distinguished into one first space, a second space and the 3rd space, the first entrance
Connect first space and positioned at the lower section of the packed bed and be used to receive a mixing liquid, the mixing liquid bag
Containing a high boiling substance, a mid boiling point materials and a low-boiling point material；
One primary heater, there is provided heat gives first space；
One secondary heater, there is provided heat gives the second space；
One first pump, is connected to the bulkhead type destilling tower, and be used to extract out in the second space in steam state
The mid boiling point materials；
One first condenser, is connected to first pump, and is used to condense by the mid-boiling point of first pumped
Material；
One second pump, is connected to one first bottom in first space, with extract out in first space in liquid
The high boiling substance of state；
One the 3rd pump, is connected to one second bottom of the second space, with extract out in the second space in liquid
The mid boiling point materials of state；And
One second condenser, is connected to the bulkhead type destilling tower, and is used to condense from the discharge of the 3rd space
In the low-boiling point material of steam state.
2. a kind of separator, it is characterised in that including：
One first entrance；
One first destilling tower, including a second entrance, the second entrance are used to receive a waste gas, the waste gas bag
Containing a high boiling substance, a mid boiling point materials and a low-boiling point material；
One after-fractionating tower；
One primary heater, there is provided first space of heat to the after-fractionating tower；
One secondary heater, there is provided the second space of heat to the after-fractionating tower；
One second pump, is connected to one first bottom of the after-fractionating tower, is in extract out in first bottom
The high boiling substance of liquid；
One the 3rd pump, is connected to one second bottom of the after-fractionating tower, is in extract out in second bottom
The mid boiling point materials of liquid；
One the 4th pump, connects first destilling tower and the after-fractionating tower, and be used to extract first destilling tower out
A bottom in the waste gas a concentrate, and be delivered to the first entrance；
One second condenser, connects first destilling tower, and is used to be arranged from the one of first destilling tower top
The waste gas condensation for going out is into a storing liquid；
One first accumulator tank, is used to store the storing liquid；And
One the 5th pump, connects first destilling tower and first accumulator tank, and be used to by the storing liquid from this
Extract and be delivered to the top of first destilling tower in one accumulator tank out.
3. separator according to claim 1 and 2, it is characterised in that the 3rd pump is more used to
The mid boiling point materials being in a liquid state being located in second bottom are delivered to the primary heater.
4. separator according to claim 2, it is characterised in that second condenser is more used to
The storing liquid will be condensed into from low-boiling point material in steam state of the one of after-fractionating tower top discharge.
5. separator according to claim 2, it is characterised in that the 5th pump is more used to this
Storing liquid is extracted out from first accumulator tank and is delivered to the top of the after-fractionating tower.
6. separator according to claim 2, it is characterised in that the first entrance located at this
Two destilling towers.
7. separator according to claim 2, it is characterised in that the first entrance located at this
Between two pumps and the primary heater.
8. separator according to claim 2, it is characterised in that the after-fractionating tower is a point
Wall type destilling tower.
9. separator according to claim 8, it is characterised in that the after-fractionating tower includes
Be distinguished into for the inside of the bulkhead type destilling tower many by packed bed, the first entrance and a demarcation strip, the demarcation strip
Individual space, the first entrance connects one of those spaces and positioned at the lower section of the packed bed.
10. separator according to claim 2, it is characterised in that the after-fractionating tower includes
Demarcation strip, the demarcation strip by the inside of the bulkhead type destilling tower be distinguished into one first space, a second space and
One the 3rd space, the first entrance and second pump connect first space, the 3rd pump and connect second sky
Between, and second condenser connects the 3rd space.
11. separators according to claim 2, it is characterised in that further include：
One the 3rd condenser, connects the after-fractionating tower, and is used to condense from a top of the after-fractionating tower
Low-boiling point material in steam state of discharge；
One second accumulator tank, is used to store the condensed low-boiling point material；
One the 6th pump, connects second accumulator tank and the after-fractionating tower, and be used to extract second accumulator tank out
Interior condensed low-boiling point material is simultaneously delivered to the top of the after-fractionating tower.
12. separators according to claim 11, it is characterised in that the 5th pump connect this
One accumulator tank and second accumulator tank.
13. separators according to claim 11, it is characterised in that the 6th pump connect this
One accumulator tank and second accumulator tank.
14. separators according to claim 2, it is characterised in that further include：
One first pump, is connected to the after-fractionating tower, and be used to extract out in the after-fractionating tower in steam state
The mid boiling point materials；And
One first condenser, is used to condense the mid boiling point materials by after first pumped.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| TW104141974 | 2015-12-14 | ||
| TW104141974 | 2015-12-14 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN106861353A true CN106861353A (en) | 2017-06-20 |
Family
ID=59238828
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510960790.2A Pending CN106861353A (en) | 2015-12-14 | 2015-12-18 | Separating device |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN106861353A (en) |
| TW (1) | TWI577436B (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107715486A (en) * | 2017-11-22 | 2018-02-23 | 广东银洋环保新材料有限公司 | A kind of emulsion VOC release units |
| CN109987660A (en) * | 2017-12-29 | 2019-07-09 | 财团法人工业技术研究院 | Solvent slop processing system and its method |
| CN110709149A (en) * | 2017-07-25 | 2020-01-17 | 阿科玛法国公司 | Method for purifying (meth) acrylic esters |
| CN112494973A (en) * | 2020-11-20 | 2021-03-16 | 湖南化工设计院有限公司 | Organic waste liquid recovery equipment and method |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2017111146A1 (en) * | 2015-12-25 | 2017-06-29 | 堺化学工業株式会社 | LOW α-RAY BARIUM SULFATE PARTICLES, USE METHOD THEREFOR, AND PRODUCTION METHOD THEREFOR |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6457703A (en) * | 1987-08-28 | 1989-03-06 | Matsushita Electric Ind Co Ltd | Metallized film capacitor |
| EP1456159B1 (en) * | 2001-12-07 | 2006-08-02 | Basf Aktiengesellschaft | Method for the isolation of trimethylol propane from a reaction mixture |
| CN101700916A (en) * | 2009-11-06 | 2010-05-05 | 清华大学 | Process and system for treating industrial normal propyl alcohol waste liquor |
| CN102256686A (en) * | 2008-12-17 | 2011-11-23 | 犹德有限公司 | Method for purifying gases and obtaining acid gases |
| CN102921180A (en) * | 2011-08-08 | 2013-02-13 | 四川西陇化工有限公司 | Preparation method of inorganic ultra-clean highly-pure reagent acid |
| CN203494195U (en) * | 2013-09-24 | 2014-03-26 | 中国石油化工股份有限公司 | Wall-dividing rectification tower applicable to azeotropic distillation |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6582564B2 (en) * | 2000-08-22 | 2003-06-24 | Sumitomo Heavy Industries, Ltd. | Distillation apparatus and distillation method |
| US7129387B2 (en) * | 2003-03-20 | 2006-10-31 | Bp Corporation North America Inc. | Low capital implementation of distributed distillation in ethylene recovery |
| TWI282746B (en) * | 2005-10-27 | 2007-06-21 | Univ Nat Taiwan | Method and apparatus for esterification |
| WO2009108419A1 (en) * | 2008-02-26 | 2009-09-03 | Dow Global Technologies Inc. | Process and apparatus for producing and purifying epichlorohydrins |
-
2015
- 2015-12-18 CN CN201510960790.2A patent/CN106861353A/en active Pending
-
2016
- 2016-03-01 TW TW105106175A patent/TWI577436B/en active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6457703A (en) * | 1987-08-28 | 1989-03-06 | Matsushita Electric Ind Co Ltd | Metallized film capacitor |
| EP1456159B1 (en) * | 2001-12-07 | 2006-08-02 | Basf Aktiengesellschaft | Method for the isolation of trimethylol propane from a reaction mixture |
| CN102256686A (en) * | 2008-12-17 | 2011-11-23 | 犹德有限公司 | Method for purifying gases and obtaining acid gases |
| CN101700916A (en) * | 2009-11-06 | 2010-05-05 | 清华大学 | Process and system for treating industrial normal propyl alcohol waste liquor |
| CN102921180A (en) * | 2011-08-08 | 2013-02-13 | 四川西陇化工有限公司 | Preparation method of inorganic ultra-clean highly-pure reagent acid |
| CN203494195U (en) * | 2013-09-24 | 2014-03-26 | 中国石油化工股份有限公司 | Wall-dividing rectification tower applicable to azeotropic distillation |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110709149A (en) * | 2017-07-25 | 2020-01-17 | 阿科玛法国公司 | Method for purifying (meth) acrylic esters |
| US11261150B2 (en) | 2017-07-25 | 2022-03-01 | Arkema France | Method for purifying (meth)acrylic esters |
| CN107715486A (en) * | 2017-11-22 | 2018-02-23 | 广东银洋环保新材料有限公司 | A kind of emulsion VOC release units |
| CN107715486B (en) * | 2017-11-22 | 2023-09-12 | 广东银洋环保新材料有限公司 | Emulsion VOC breaks away from device |
| CN109987660A (en) * | 2017-12-29 | 2019-07-09 | 财团法人工业技术研究院 | Solvent slop processing system and its method |
| CN112494973A (en) * | 2020-11-20 | 2021-03-16 | 湖南化工设计院有限公司 | Organic waste liquid recovery equipment and method |
Also Published As
| Publication number | Publication date |
|---|---|
| TW201720507A (en) | 2017-06-16 |
| TWI577436B (en) | 2017-04-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106861353A (en) | Separating device | |
| CN104334243A (en) | Dehydration of dilutions of compounds forming an azeotrope with water | |
| CN104262090B (en) | The production method of a kind of biomass dehydrated alcohol and device | |
| KR101584529B1 (en) | Solution treatment device | |
| US20120285661A1 (en) | Vapor absorption system | |
| CN104151136B (en) | The processing method of butanols-N-BUTYL ACETATE is reclaimed from antibiotic production wastewater | |
| CN201299982Y (en) | Series-connected multi-level rectification solvent recovery device | |
| CN103709022B (en) | A kind of pervaporation method reclaims technique and the device of butanone | |
| CN102128548A (en) | Method and equipment for purifying and recovering evaporated vapor obtained by drying coal | |
| RU2617506C2 (en) | Method and apparatus for distillation of methanol and heat recovery | |
| MX2012011568A (en) | Vapour absorption system. | |
| CN103215073B (en) | Production method for extracting lignite wax from brown coal | |
| CN106977409B (en) | A kind of separation method of triethylamine and water | |
| CN211445385U (en) | Contain organic solvent's salt waste water evaporation equipment | |
| CN205730432U (en) | A kind of mechanical steam recompression Distallation systm | |
| CN103484154A (en) | Condensed water stripped crude oil stabilization method and special device thereof | |
| CN103910605B (en) | The technique of a kind of infiltration evaporation system and refined biological propyl carbinol thereof | |
| CN206730550U (en) | Energy-saving continuous rectification system | |
| CN207012590U (en) | A kind of dehydration of organic solvent system | |
| CN102172435B (en) | Tandem multistage continuous rectification solvent recoverer | |
| CN206980184U (en) | A kind of Pervaporation membrane dehydration of organic solvent equipment | |
| CN103007565B (en) | Method and device for triple-effect separation of methylbenzene and polyethylene | |
| CN201978519U (en) | Series type multi-stage continuous rectification solvent recoverer | |
| CN108863723A (en) | The power-economizing method and its device of distillation process in a kind of cyclohexanol production | |
| JP6312614B2 (en) | Hydrous ethanol distillation apparatus and method for producing absolute ethanol |
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 | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20170620 |
|
| WD01 | Invention patent application deemed withdrawn after publication |