CN113860994B - Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method - Google Patents
Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method Download PDFInfo
- Publication number
- CN113860994B CN113860994B CN202111275823.1A CN202111275823A CN113860994B CN 113860994 B CN113860994 B CN 113860994B CN 202111275823 A CN202111275823 A CN 202111275823A CN 113860994 B CN113860994 B CN 113860994B
- Authority
- CN
- China
- Prior art keywords
- tank
- product
- acid
- raw material
- membrane separation
- 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
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 112
- 239000012528 membrane Substances 0.000 title claims abstract description 61
- 238000000926 separation method Methods 0.000 title claims abstract description 43
- 238000006386 neutralization reaction Methods 0.000 title claims abstract description 19
- 238000010168 coupling process Methods 0.000 title claims abstract description 12
- 238000000034 method Methods 0.000 title abstract description 20
- 239000000047 product Substances 0.000 claims abstract description 40
- 239000002994 raw material Substances 0.000 claims abstract description 36
- 230000003068 static effect Effects 0.000 claims abstract description 30
- 238000001514 detection method Methods 0.000 claims abstract description 23
- 239000003513 alkali Substances 0.000 claims abstract description 19
- 239000012466 permeate Substances 0.000 claims abstract description 19
- 239000002585 base Substances 0.000 claims abstract description 17
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000000872 buffer Substances 0.000 claims abstract description 15
- 239000011552 falling film Substances 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 11
- 230000002378 acidificating effect Effects 0.000 claims abstract description 7
- 230000007935 neutral effect Effects 0.000 claims abstract description 6
- 239000002904 solvent Substances 0.000 claims description 19
- 239000002808 molecular sieve Substances 0.000 claims description 12
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 9
- 238000004519 manufacturing process Methods 0.000 claims description 9
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 6
- 239000012071 phase Substances 0.000 claims description 6
- 239000012510 hollow fiber Substances 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 229910000030 sodium bicarbonate Inorganic materials 0.000 claims description 3
- 235000017557 sodium bicarbonate Nutrition 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims description 2
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims 1
- 230000000149 penetrating effect Effects 0.000 claims 1
- 235000019441 ethanol Nutrition 0.000 abstract description 30
- 239000000463 material Substances 0.000 abstract description 7
- 150000003839 salts Chemical class 0.000 abstract description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 3
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 239000010408 film Substances 0.000 abstract 1
- 239000011259 mixed solution Substances 0.000 description 19
- 239000000243 solution Substances 0.000 description 12
- 239000000126 substance Substances 0.000 description 7
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- QUSNBJAOOMFDIB-UHFFFAOYSA-N Ethylamine Chemical compound CCN QUSNBJAOOMFDIB-UHFFFAOYSA-N 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000012465 retentate Substances 0.000 description 2
- UIIMBOGNXHQVGW-DEQYMQKBSA-M Sodium bicarbonate-14C Chemical compound [Na+].O[14C]([O-])=O UIIMBOGNXHQVGW-DEQYMQKBSA-M 0.000 description 1
- IKHGUXGNUITLKF-XPULMUKRSA-N acetaldehyde Chemical compound [14CH]([14CH3])=O IKHGUXGNUITLKF-XPULMUKRSA-N 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- 238000010533 azeotropic distillation Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a device and a process method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method. The device comprises a raw material tank, a preheater, a falling film evaporator, a superheater, a vapor permeable membrane separation device, a product condenser, a permeate condenser, a vacuum buffer tank, a vacuum unit, a liquid alkali tank, a metering pump, a pipeline static mixer, a detection tank and a conveying pump. The technological process includes the steps of conveying acid-containing material and alkali liquid into a static mixer for neutralization, conveying the neutralized product into a detection tank, heat exchanging the neutral or weak alkaline material from the detection tank, eliminating alkali matter and salt in a falling film evaporator to obtain material vapor, heating the material vapor to 110-150 deg.c, and separating in a vapor permeation film separator to obtain high purity ethanol product and permeating liquid. The water content in the product ethanol can be reduced to below 0.5wt.% by adopting the device and the process for treating the aqueous acidic ethanol raw material liquid.
Description
Technical Field
The invention belongs to the field of ethanol production, and particularly relates to a device and a method for preparing absolute ethanol by an acid-base neutralization and membrane separation coupling method.
Background
The absolute ethyl alcohol is an ethanol product with the ethanol content of more than or equal to 99.5 percent, plays a role in modern industry, can be widely used as an organic solvent in the industries of pharmaceutical chemical industry, fine chemical industry, energy, electronics, environmental protection, food and the like, and is used as an important basic chemical and chemical raw material for producing acetaldehyde, acetic acid, ethylamine, ethyl acetate and the like. The traditional organic solvent dehydration method mainly comprises azeotropic distillation, extractive distillation, adsorption and other methods. The membrane refining dewatering separation process is one new type of membrane separation technology for dewatering organic solvent, and the process is one separation process with different component vapor partial pressure difference in liquid mixture and inorganic membrane material to realize separation. However, the inorganic membrane material cannot process acidic raw material liquid due to the material characteristics, and the service life of the membrane is greatly reduced, so that the application range of the membrane separation method is limited.
Disclosure of Invention
The invention aims to provide a device and a process method for preparing absolute ethyl alcohol by an acid-base neutralization and membrane separation coupling method. By coupling the acid-base neutralization process with the membrane separation, the pH value of the raw material liquid entering the membrane separation unit is effectively ensured. By adopting the process to treat the aqueous acidic ethanol raw material liquid, the water content in the ethanol product can be reduced to below 0.5 wt.%.
In order to achieve the above purpose, the present invention is specifically achieved by the following technical scheme.
The invention provides a device for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method, which comprises the following steps: comprising the following steps: feed tank, charge-in pump, pre-heater, falling film evaporator, superheater, vapor permeation membrane separation device, product condenser, product tank, permeate condenser, vacuum buffer tank, vacuum unit, wherein: the device also comprises an alkali solution tank, a metering pump, a pipeline static mixer, a detection tank and a delivery pump; the raw material tank, the feed pump and the pipeline static mixer are sequentially communicated through pipelines; the alkali liquid tank, the metering pump and the pipeline static mixer are sequentially communicated through pipelines; the outlet of the pipeline static mixer, the detection tank, the delivery pump, the preheater, the falling film evaporator, the superheater and the vapor permeation membrane separation device are sequentially communicated through pipelines; the product side outlet of the steam permeable membrane separation device, the preheater, the product condenser and the product tank are sequentially communicated through pipelines; and a permeate outlet of the steam permeable membrane separation device, a permeate condenser, a vacuum buffer tank and a vacuum unit are sequentially communicated through pipelines.
Further, the vapor permeable membrane configuration of the vapor permeable membrane separation device comprises a tubular, hollow fiber type.
Further, the vapor permeable membrane is an organic or inorganic membrane, and comprises a NaA molecular sieve membrane, a T-shaped molecular sieve membrane, a MOR molecular sieve membrane and a ZSM-5 molecular sieve membrane.
The invention also provides a process for preparing absolute ethyl alcohol by using the acid-base neutralization-membrane separation coupling method, which comprises the following steps:
the method comprises the steps that acid-containing raw materials to be treated are conveyed to a pipeline static mixer from a raw material tank through a feed pump, meanwhile, alkali liquor with certain concentration is conveyed to the pipeline static mixer from an alkali liquor tank through a metering pump, acid-base neutralization is carried out on the acid-containing raw materials and the alkali liquor in the pipeline static mixer, the neutralized raw materials enter a detection tank, and the pH value is detected in real time through an online remote pH meter; if the solvent in the detection tank is neutral or weak alkaline, the solvent is qualified, and the qualified solvent is conveyed to the preheater through a pump; if the solvent in the detection tank is acidic, the solvent is an unqualified solvent, the unqualified solvent is pumped back to the pipeline mixer by a pump, and the unqualified acidic solvent is further subjected to acid-base neutralization reaction in the pipeline static mixer until the pH value of the solvent is qualified; the qualified neutral or weak alkaline raw material from the buffer tank is pressurized by a delivery pump, enters a raw material preheater to exchange heat with product steam, enters a falling film evaporator, is heated and vaporized by saturated steam, discharges concentrated solution at the bottom of the evaporator, and removes alkaline substances and salts dissolved in the solution through the concentrated acid discharge of the falling film evaporator. Meanwhile, raw material steam is heated to 110-150 ℃ by a heater and then enters a membrane component for separation, the separated trapped components enter a preheater to exchange heat with raw material liquid, then enter a product condenser for further cooling, and enter a product tank; the permeate enters a permeate condenser to exchange heat with a low-temperature refrigerant, the liquid phase enters a vacuum buffer tank, and the gas phase maintains the vacuum pressure of about 1KPaA through a vacuum pump unit.
Further, the acid-containing raw material to be treated is acid ethanol with the concentration of 85-99% (V/V), H + The concentration is 1000ppm or less.
Further, the alkali liquor is 10-50% sodium hydroxide, calcium hydroxide, sodium bicarbonate, sodium carbonate and other solutions.
Further, the pH value of the qualified solvent in the detection tank is 7.0-8.0.
Further, the temperature of the preheated preheater is 65-85 ℃.
Further, the raw material steam is heated by a heater and then enters a membrane assembly for separation, the separated retentate component membrane retentate obtains high-purity ethanol steam with the concentration reaching 99.5-99.9% (V/V), the dehydrated ethanol steam is condensed to obtain an ethanol product, and the ethanol content in the permeate liquid at the permeate side is 1-5% (V/V).
The device and the process method effectively ensure the pH value of the raw material liquid entering the membrane separation unit by coupling the acid-base neutralization process and the membrane separation. The water content in the ethanol product can be reduced to below 0.5wt.% by adopting the process to treat the aqueous acidic ethanol raw material liquid.
Drawings
FIG. 1 is a flow chart of a process for preparing absolute ethanol by an acid-base neutralization-membrane separation coupling method according to an embodiment of the invention.
Wherein: 1 is a raw material tank; 2 is a feed pump; 3 is an alkali solution tank; 4 is a metering pump; 5 is a pipe static mixer; 6 is a detection tank; 7 is a transfer pump; 8 is a preheater; 9 is a falling film evaporator; 10 is a superheater; 11 is a vapor permeable membrane separation device; 12 is a product condenser; 13 is a product tank; 14 is a permeate condenser; 15 is a vacuum buffer tank; 16 is a vacuum unit.
Detailed Description
For further explanation of the technical solution of the present invention, the following specific examples are given. It should be noted that the present invention has been described by way of example and illustration only, and various modifications, additions and substitutions to the described embodiments may be made by those skilled in the art without departing from the spirit of the invention or exceeding the scope of the invention as defined in the accompanying claims.
The core of the specific embodiment of the invention is to provide a device for preparing absolute ethyl alcohol by an acid-base neutralization and membrane separation coupling method (shown in figure 1), which comprises a raw material tank 1, a feed pump 2, an alkali liquid tank 3, a metering pump 4, a pipeline static mixer 5, a detection tank 6, a delivery pump 7, a preheater 8, a falling film evaporator 9, a superheater 10, a steam permeable membrane separation device 11, a product condenser 12, a product tank 13, a permeate condenser 14, a vacuum buffer tank 15 and a vacuum unit 16. The raw material tank 1, the feed pump 2 and the pipeline static mixer 5 are sequentially communicated through pipelines; the alkali solution tank 3, the metering pump 4 and the pipeline static mixer 5 are sequentially communicated through pipelines; the outlet of the pipeline static mixer 5, the detection tank 6, the delivery pump 7, the preheater 8, the falling film evaporator 9, the superheater 10 and the vapor permeation membrane separation device 11 are sequentially communicated through pipelines; the product side outlet of the vapor permeable membrane separation device 11, the preheater 8, the product condenser 12 and the product tank 13 are sequentially communicated through pipelines; the permeate outlet of the vapor permeable membrane separation device 11, the permeate condenser 14, the vacuum buffer tank 15, and the vacuum unit 16 are sequentially connected through pipelines.
Example 1
Ethanol content of 85% (V/V), H + The mixed raw material with the content of 1000ppm is conveyed to a pipeline static mixer through a feed pump, 50% sodium hydroxide solution is used for acid-base neutralization in the pipeline static mixer through a metering pump to a detection tank, weak alkaline mixed solution with the pH value of 8.0 is obtained, the weak alkaline mixed solution is conveyed to a preheater through a conveying pump and preheated to 90 ℃, raw material steam and concentrated solution are obtained through a falling film evaporator, alkaline substances and inorganic salts in the mixed solution are removed through an outward concentrated solution, the raw material steam is continuously heated to 150 ℃ through the heater, the raw material steam enters a tubular NaA molecular sieve membrane separation device, ethanol gas at the product side and the preheater are subjected to heat exchange and cooling, and then are further cooled through a condenser to obtain an ethanol product with the purity of 99.5% (V/V), after condensation, the mixed solution at the permeate side is stored in a vacuum buffer tank, the ethanol content is 1% (V/V), and the gas phase is pumped away through a vacuum unit.
Example 2
Ethanol content of 90% (V/V), H + The mixed raw material with the content of 800ppm is conveyed to a pipeline static mixer through a feed pump, 30% calcium hydroxide solution is used for acid-base neutralization in the pipeline static mixer through a metering pump to a detection tank, weak alkaline mixed solution with the pH value of 7.8 is obtained, the weak alkaline mixed solution is conveyed to a preheater through a conveying pump and preheated to 80 ℃, alkaline substances and inorganic salts in the mixed solution are removed through a membrane evaporator, the mixed solution is continuously heated to 130 ℃ through the superheater, the mixed solution enters a hollow fiber type T-shaped molecular sieve membrane separation device, ethanol gas at the product side is cooled by a condenser after heat exchange with the preheater, the ethanol product is obtained, the purity is 99.7% (V/V), the mixed solution at the permeation side is stored in a vacuum buffer tank after being condensed, the ethanol content is 2% (V/V), and the gas phase is pumped out through a vacuum unit.
Example 3
Ethanol content of 95% (V/V), H + The mixed raw material with the content of 600ppm is conveyed to a pipeline static mixer through a feed pump, 20% sodium bicarbonate solution is used for acid-base neutralization in the pipeline static mixer through a metering pump to a detection tank, weak alkaline mixed solution with the pH value of 7.6 is obtained, the weak alkaline mixed solution is conveyed to a preheater through a conveying pump and preheated to 65 ℃, alkaline substances and inorganic salts in the mixed solution are removed through a membrane evaporator, the mixed solution is continuously heated to 110 ℃ through the superheater, the mixed solution enters a tubular MOR molecular sieve membrane separation device, ethanol gas at the product side and the preheater are subjected to heat exchange and cooling, and then are further cooled through a condenser to obtain an ethanol product, the purity is 99.8% (V/V), the mixed solution at the permeate side is condensed, the liquid phase is stored in a vacuum buffer tank, the ethanol content is 3% (V/V), and the gas phase is pumped through a vacuum unit.
Example 4
Ethanol content of 99% (V/V), H + The mixed raw material with the content of 200ppm is conveyed to a pipeline static mixer through a feed pump, 10 percent sodium bicarbonate solution is used for acid-base neutralization in the pipeline static mixer through a metering pump to a detection tank to obtain weak alkaline mixed solution with the pH value of 7.2, the weak alkaline mixed solution is conveyed to a preheater through a conveying pump and preheated to 70 ℃, alkaline substances and inorganic salts in the mixed solution are removed through a membrane evaporator,continuously heating to 120 ℃ through a heater, entering a hollow fiber type ZSM-5 molecular sieve membrane separation device, carrying out heat exchange and cooling on the ethanol gas at the product side and the preheater, further cooling through a condenser to obtain an ethanol product, condensing the mixed liquid at the permeation side, storing the liquid phase in a vacuum buffer tank, wherein the ethanol content is 5% (V/V), and pumping the gas phase through a vacuum unit.
The above embodiments are only for illustrating the technical concept and features of the present invention, and are intended to enable those skilled in the art to understand the content of the present invention and implement the same according to the content of the present invention, and are not intended to limit the scope of the present invention. All equivalent changes or modifications made in accordance with the spirit of the present invention should be construed to be included in the scope of the present invention.
The invention is not a matter of the known technology.
Claims (7)
1. The utility model provides a device of neutralization of acid and alkali and membrane separation coupling method anhydrous ethanol, includes head tank, pre-heater, falling film evaporator, superheater, vapor permeation membrane separation device, product condenser, permeate condenser, vacuum buffer tank, vacuum unit, feed pump, product tank, its characterized in that: the device also comprises an alkali solution tank, a metering pump, a pipeline static mixer, a detection tank and a delivery pump, wherein the raw material tank, the feed pump and the pipeline static mixer are sequentially communicated through pipelines; the alkali liquid tank, the metering pump and the pipeline static mixer are sequentially communicated through pipelines; the outlet of the pipeline static mixer, the detection tank, the delivery pump, the preheater, the falling film evaporator, the superheater and the vapor permeation membrane separation device are sequentially communicated through pipelines; the product side outlet of the steam permeable membrane separation device, the preheater, the product condenser and the product tank are sequentially communicated through pipelines; the permeate outlet, the permeate condenser, the vacuum buffer tank and the vacuum unit of the vapor permeable membrane separation device are sequentially communicated through pipelines; the steam permeable membrane of the steam permeable membrane separation device is configured to be tubular or hollow fiber; the vapor permeable membrane is an organic or inorganic membrane and comprises a NaA molecular sieve membrane, a T-shaped molecular sieve membrane, a MOR molecular sieve membrane and a ZSM-5 molecular sieve membrane.
2. A process for preparing absolute ethanol using the apparatus of claim 1, comprising the steps of:
the acid-containing raw material and the alkali liquor are respectively conveyed into a pipeline static mixer through a feed pump and a metering pump, the acid-containing raw material and the alkali liquor are subjected to acid-alkali neutralization in the pipeline static mixer, and the neutralized product enters a detection tank, and the pH value is detected in real time through an online remote pH meter; if the solvent in the detection tank is neutral or weak alkaline, the solvent is qualified, and the qualified solvent is conveyed to the preheater through a pump; if the solvent in the detection tank is acidic, the solvent is an unqualified solvent, the unqualified solvent is pumped back to the pipeline static mixer through a pump, and acid-base neutralization reaction is further carried out until the pH value of the solvent is qualified; the neutral or weak alkaline raw material from the detection tank is pressurized by a delivery pump, enters a preheater to exchange heat with product steam, enters a falling film evaporator, is heated and vaporized by saturated steam to obtain raw material steam, and the bottom of the falling film evaporator is discharged with concentrated solution; meanwhile, raw material steam is heated to 110-150 ℃ through a heater and then enters a steam permeation membrane separation device for separation, the separated trapped components enter a preheater for heat exchange with raw material liquid, then enter a product condenser for further cooling, and enter a product tank; and (3) allowing the separated permeate to enter a permeate condenser for heat exchange with a low-temperature refrigerant, allowing a liquid phase to enter a vacuum buffer tank, and allowing a gas phase to maintain vacuum pressure of 1KPaA through a vacuum unit.
3. The process for preparing absolute ethanol according to claim 2, characterized in that: the acid-containing raw material is acid ethanol with the volume concentration of 85-99%, H + The concentration is 1000ppm or less.
4. The process for preparing absolute ethanol according to claim 2, characterized in that: the alkali liquor is 10-50% sodium hydroxide, calcium hydroxide, sodium bicarbonate and sodium carbonate solution.
5. The process for preparing absolute ethanol according to claim 2, characterized in that: and the pH value of the neutral or weak alkaline qualified solvent in the detection tank is 7.0-8.0.
6. The process for preparing absolute ethanol according to claim 2, characterized in that: the temperature of the preheated preheater is 65-85 ℃.
7. The process for preparing absolute ethanol of claim 2, wherein: the volume content of the ethanol in the penetrating fluid is 1-5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111275823.1A CN113860994B (en) | 2021-10-29 | 2021-10-29 | Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111275823.1A CN113860994B (en) | 2021-10-29 | 2021-10-29 | Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113860994A CN113860994A (en) | 2021-12-31 |
| CN113860994B true CN113860994B (en) | 2024-02-09 |
Family
ID=78986231
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111275823.1A Active CN113860994B (en) | 2021-10-29 | 2021-10-29 | Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113860994B (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| CN105218316A (en) * | 2014-11-28 | 2016-01-06 | 杭州奇纯膜技术有限公司 | A kind of hollow fiber pervaporation membrane prepares the device and method of dehydrated alcohol |
| CN206980472U (en) * | 2017-06-21 | 2018-02-09 | 武汉智宏思博化工科技有限公司 | A kind of industrial equipment of Pervaporation membrane and the tower-coupled production absolute ethyl alcohol of rectifying |
| CN110294665A (en) * | 2019-07-09 | 2019-10-01 | 常州制药厂有限公司 | The recyclable device and recovery method of ethyl alcohol in Doxycycline Hyclate refinement mother liquor |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8128826B2 (en) * | 2007-02-28 | 2012-03-06 | Parker Filtration Bv | Ethanol processing with vapour separation membranes |
-
2021
- 2021-10-29 CN CN202111275823.1A patent/CN113860994B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104262090A (en) * | 2014-09-22 | 2015-01-07 | 江苏九天高科技股份有限公司 | Method and device for producing biomass absolute ethyl alcohol |
| CN105218316A (en) * | 2014-11-28 | 2016-01-06 | 杭州奇纯膜技术有限公司 | A kind of hollow fiber pervaporation membrane prepares the device and method of dehydrated alcohol |
| CN206980472U (en) * | 2017-06-21 | 2018-02-09 | 武汉智宏思博化工科技有限公司 | A kind of industrial equipment of Pervaporation membrane and the tower-coupled production absolute ethyl alcohol of rectifying |
| CN110294665A (en) * | 2019-07-09 | 2019-10-01 | 常州制药厂有限公司 | The recyclable device and recovery method of ethyl alcohol in Doxycycline Hyclate refinement mother liquor |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113860994A (en) | 2021-12-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| WO2011027787A1 (en) | Method for dewatering water-containing organic substance | |
| CN110282676B (en) | Hydrazine hydrate wastewater evaporation crystallization equipment and evaporation crystallization process thereof | |
| CN103922529B (en) | Low-energy-consumption device for recycling hydrochloric acid waste water and method for recycling hydrochloric acid waste water | |
| CN110938047B (en) | Tetrahydrofuran-benzene-water mixture separation process and device | |
| CN110698324A (en) | Device and novel process for producing fuel ethanol and electronic grade ethanol by rectification-membrane separation coupling method | |
| CN102838134B (en) | Sal prunella coproduction technology and device adopting sodium sulfate type bittern mechanical vapour recompression method | |
| CN113860994B (en) | Device and method for preparing absolute ethyl alcohol by acid-base neutralization and membrane separation coupling method | |
| CN111470563A (en) | DMF (dimethyl formamide) or DMAC (dimethylacetamide) waste gas and wastewater series treatment system and method | |
| CN103657136A (en) | Method and equipment for evaporative crystallization of aluminium chloride | |
| CN104193651A (en) | Refining method and device for synthesizing acetonitrile from acetic acid by ammoniation | |
| CN102107119A (en) | Multiple-effect membrane distillation device and method | |
| CN114436293B (en) | Method for directly producing sodium bromide from low-concentration brine | |
| CN112062655A (en) | Deep dehydration method for ethanol | |
| CN111848348A (en) | Isopropyl alcohol dehydration refining method | |
| CN105923673A (en) | Adipic acid waste water evaporation and concentration process and device thereof | |
| CN106831380B (en) | Method for dehydrating and concentrating formaldehyde solution | |
| CN206940774U (en) | A kind of tetrahydrofuran dehydration device | |
| CN111909120B (en) | Energy-saving separation process of water-containing ternary azeotropic system | |
| CN105622617B (en) | A method of sildenafil citrate mother liquor is subjected to cleaning recycling | |
| CN103450001A (en) | Method and equipment for concentrating sodium formate in pentaerythritol production | |
| CN110787638B (en) | Concentration system and concentration method of pentanediamine | |
| CN210635842U (en) | Reverse osmosis concentrated water concentration and reduction device | |
| KR101985444B1 (en) | Method of recovering highly concentrated formic acid and highly concentrated sulfate from formate aqueous solution, and recovery apparatus | |
| CN217909007U (en) | Cellulose solvent recovery device | |
| CN107011246B (en) | Method for dehydrating and desalting triacetonamine synthetic liquid |
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 | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |