CN211612282U - Triple-effect membrane separation dehydration energy-saving device for preparing anhydrous alcohol - Google Patents
Triple-effect membrane separation dehydration energy-saving device for preparing anhydrous alcohol Download PDFInfo
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- CN211612282U CN211612282U CN201922437142.5U CN201922437142U CN211612282U CN 211612282 U CN211612282 U CN 211612282U CN 201922437142 U CN201922437142 U CN 201922437142U CN 211612282 U CN211612282 U CN 211612282U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
Abstract
The utility model discloses a triple effect membrane separation dehydration economizer for preparing anhydrous alcohol, the device includes raw materials pre-heater, reboiler, finished product cooler, first alcohol evaporation dewatering system, second alcohol evaporation dewatering system and third alcohol evaporation dewatering system. And (3) respectively feeding the raw material alcohol into three alcohol evaporation and dehydration systems for distillation, dehydration and purification to obtain the finished product anhydrous alcohol. The steam heat is used in series between the three systems. The utility model discloses a triple effect thermal coupling dehydration technology utilizes the anhydrous alcohol steam of previous effect as the heat source of the raw materials alcohol evaporator of next effect, has realized thermal reuse, can also not consume unnecessary energy and just concentrate the recovery with weak alcohol. The steam consumption of the anhydrous alcohol per ton is not more than 0.2 ton, and compared with the single-effect pervaporation membrane separation dehydration process, the energy is saved by more than 55%.
Description
Technical Field
The utility model relates to an alcohol production technology technical field especially relates to a triple effect membrane separation dehydration economizer for preparing anhydrous alcohol.
Background
In recent years, the country has vigorously popularized fuel ethanol, and an implementation scheme about expansion of biofuel ethanol production and popularization and use of vehicle ethanol gasoline is proposed in 15 ministers such as 2017 co-issued by national reform and committee of the nation, so that the aim of achieving national basic coverage of ethanol gasoline in 2020 is fulfilled. The general service meeting is held in a state hospital of 8, month and 22 in 2018, and the state meeting at that time determines that the vehicle ethanol gasoline is orderly popularized and used, and is popularized in 26 provinces and cities in China. At present, the production capacity of fuel ethanol in China is less than 300 million tons, the consumption of gasoline in China is about 1.3 million tons at present, the fuel ethanol is calculated according to the addition proportion of 10 percent, if the national basic coverage is realized in 2020, the demand of the fuel ethanol is 1300 million tons, the gap reaches 1000 million tons, and the market potential is huge.
At present, the domestic and foreign alcohol dehydration technology mainly comprises four methods:
(1) the method for dehydrating by adopting the azeotropic distillation of benzene or cyclohexane has high energy consumption, and the product is easy to have benzene or cyclohexane residues and is gradually eliminated.
(2) The method has the advantages of no residue, good product quality and high energy consumption by adopting glycol salt-adding extraction dehydration.
(3) The molecular sieve adsorption method is adopted for dehydration, and the method has the advantages of no residue, high product concentration and relatively low energy consumption.
(4) By adopting the pervaporation membrane separation technology, the method has no residue and low energy consumption.
Under the situation of increasingly short energy sources, the requirement on energy consumption is higher and higher, and an alcohol dehydration technology with lower energy consumption is needed.
SUMMERY OF THE UTILITY MODEL
The utility model provides a triple effect membrane separation dehydration economizer for preparing anhydrous alcohol to prior art's not enough. By adopting a three-effect thermal coupling dehydration process and using the anhydrous alcohol vapor of the former effect as the heat source of the raw material alcohol evaporator of the latter effect, the heat is recycled.
The utility model discloses a realize through following technical scheme:
the utility model provides a triple-effect membrane separation dehydration energy-saving device for preparing anhydrous alcohol, which comprises a raw material preheater; the raw material preheater is connected with a first alcohol evaporation dehydration system through a first alcohol feeding pipe, the raw material preheater is connected with a second alcohol evaporation dehydration system through a second alcohol feeding pipe, and the raw material preheater is connected with a third alcohol evaporation dehydration system through a third alcohol feeding pipe; the reboiler is connected with a first alcohol evaporation and dehydration system through a first reboiler pipe, and the first alcohol evaporation and dehydration system is connected with a second alcohol evaporation and dehydration system through a first anhydrous alcohol steam pipe; the second alcohol evaporation dehydration system is connected with the third alcohol evaporation dehydration system through a second anhydrous alcohol steam pipe; the second alcohol evaporation dehydration system is sequentially connected with the first alcohol evaporation dehydration system and the finished product cooler through a first alcohol discharge pipe, the third alcohol evaporation dehydration system is sequentially connected with the second alcohol evaporation dehydration system and the finished product cooler through a second alcohol discharge pipe, and the third alcohol evaporation dehydration system is connected with the finished product cooler through a third anhydrous alcohol steam pipe;
the first alcohol evaporation dehydration system comprises a first-effect evaporation recovery tower and a first-effect membrane assembly; the upper part of the primary-effect evaporation recovery tower is sequentially connected with a primary-effect feeding secondary preheater, a primary-effect feeding primary preheater and a raw material preheater through a first alcohol feeding pipe, and the top of the primary-effect evaporation recovery tower is connected with a primary-effect membrane assembly; the bottom of the primary evaporation recovery tower is connected with a light alcohol secondary preheater;
the second alcohol evaporation dehydration system comprises a double-effect evaporator and a double-effect membrane component; the middle part of the second-effect evaporator is sequentially connected with a second-effect feeding secondary preheater, a second-effect feeding primary preheater and a raw material preheater through a second alcohol feeding pipe, and the top part of the second-effect evaporator is connected with a second-effect membrane assembly;
the third alcohol evaporation dehydration system comprises a triple-effect evaporator and a triple-effect membrane assembly; the middle part of the triple-effect evaporator is sequentially connected with a triple-effect feed preheater and a raw material preheater through a third alcohol feed pipe, and the top part of the triple-effect evaporator is connected with the triple-effect membrane assembly.
Preferably, the top of the primary-effect evaporation recovery tower is connected with the primary-effect membrane assembly through a primary-effect superheater; the top of the double-effect evaporator is connected with the double-effect membrane component through a double-effect superheater; the top of the triple-effect evaporator is connected with the triple-effect membrane component through a triple-effect superheater.
Preferably, the first-effect membrane assembly is connected with the upper part of the second-effect evaporator through a first anhydrous alcohol steam pipe; the second-effect membrane assembly is connected with the upper part of the third-effect evaporator through a second anhydrous alcohol steam pipe; the triple-effect membrane assembly is sequentially connected with the raw material preheater, the triple-effect condenser and the finished product cooler through a third absolute alcohol pipe.
Preferably, the lower part of the second-effect evaporator is sequentially connected with a first-effect feeding first-stage preheater, a light alcohol first-stage preheater and a finished product cooler through a first alcohol discharge pipe; the lower part of the triple-effect evaporator is sequentially connected with a double-effect feeding primary preheater and a finished product cooler through a second alcohol discharging pipe.
Preferably, the first-effect membrane assembly is sequentially connected with a first-effect analysis condenser, a first-stage light alcohol preheater and a second-stage light alcohol preheater through pipelines and then connected with the middle part of the first-effect evaporation recovery tower; the double-effect membrane component is connected with the primary light alcohol preheater through a double-effect desorption condenser; the triple-effect membrane component is connected with the primary light alcohol preheater through a triple-effect desorption condenser.
Preferably, the reboiler and the primary-effect evaporation recovery tower are respectively connected through a first reboiler pipe and a water return pipe, and the reboiler is sequentially connected with the primary-effect feeding secondary preheater, the secondary-effect feeding secondary preheater and the tertiary-effect feeding preheater through a second reboiler pipe.
The second aspect of the present invention provides an energy saving method for preparing anhydrous alcohol, comprising the steps of:
(1) the steam enters a reboiler, the water returned from the first-effect evaporation recovery tower is heated to 160 ℃ under the pressure of 0.6MPa, and then enters the first-effect evaporation recovery tower to be hot water at 153 ℃, so that heat is provided for the first-effect evaporation recovery tower to evaporate the raw material alcohol; condensed water in the shell pass of the reboiler enters a primary-effect feeding secondary preheater, heat is provided for the primary-effect feeding secondary preheater to enable the temperature to reach 125 ℃, hot water after the primary-effect feeding secondary preheater is heated enters a secondary-effect feeding secondary preheater again to enable the temperature to reach 113 ℃, hot water after the secondary-effect feeding secondary preheater is heated enters a tertiary-effect feeding preheater again to enable the temperature to reach 100 ℃ for the tertiary-effect feeding preheater;
(2) raw material alcohol enters a raw material preheater to be preheated to 80 ℃, and then is divided into three parts: a first raw material alcohol, a second raw material alcohol and a third raw material alcohol;
(3) the method comprises the following steps that first raw material alcohol enters a first-effect feeding first-stage preheater to be heated to 115 ℃, then enters a first-effect feeding second-stage preheater to be heated to 125 ℃, finally enters a first-effect evaporation recovery tower to be evaporated to obtain alcohol steam at 125 ℃, the alcohol steam at 125 ℃ is changed into superheated alcohol steam through a first-effect superheater, the superheated alcohol steam enters a first-effect membrane assembly to be dehydrated to obtain first anhydrous alcohol steam, the first anhydrous alcohol steam enters a second-effect evaporator to provide heat for the second-effect evaporator, the temperature of the second-effect evaporator is maintained at 118 ℃, then the first-effect feeding first-stage preheater is used for maintaining the temperature of the first-effect feeding first-stage preheater, then the first anhydrous alcohol steam enters a fresh alcohol first-stage preheater to provide heat for the fresh alcohol first-stage preheater, and finally the first-;
the second raw material alcohol enters a secondary-effect feeding primary preheater to be heated to 108 ℃, then enters a secondary-effect feeding secondary preheater to be heated to 113 ℃, finally enters a secondary-effect evaporator to be evaporated to obtain 118 ℃ alcohol steam, the 118 ℃ alcohol steam is changed into superheated alcohol steam through a secondary-effect superheater and enters a secondary-effect membrane assembly to be dehydrated to obtain second anhydrous alcohol steam, the second anhydrous alcohol steam enters a tertiary-effect evaporator to provide heat for the tertiary-effect evaporator, the temperature of the tertiary-effect evaporator is maintained at 112 ℃, then enters the secondary-effect feeding primary preheater to maintain the temperature of the secondary-effect feeding primary preheater, and finally enters a finished product cooler to be cooled to obtain anhydrous alcohol;
the third raw material spirit enters a triple-effect feeding preheater to be heated to 100 ℃, then enters a triple-effect evaporator to be evaporated to obtain 112 ℃ alcohol steam, the 112 ℃ alcohol steam is changed into superheated alcohol steam through a triple-effect superheater and enters a triple-effect membrane assembly to be dehydrated to obtain third anhydrous alcohol steam, the third anhydrous alcohol steam enters a raw material preheater to provide heat for the raw material preheater, and then enters a finished product cooler to be cooled after being condensed by a triple-effect condenser to obtain anhydrous alcohol;
(4) the first-effect membrane assembly is used for dehydrating alcohol steam and separating water steam containing a small amount of anhydrous alcohol, the water steam enters a first-effect analysis condenser to be changed into the light alcohol, the light alcohol enters a first-effect preheater and a second-effect preheater of the light alcohol and then is gradually heated, and finally the light alcohol enters the middle part of a first-effect evaporation recovery tower, the anhydrous alcohol and water are separated from the light alcohol, the anhydrous alcohol is evaporated and recovered, and the water enters the bottom of the first-effect evaporation recovery tower and enters a reboiler through a water return pipe to be heated to 160 ℃ for recycling;
the water vapor containing a small amount of anhydrous alcohol separated by the double-effect membrane component enters a double-effect analysis condenser to be changed into light alcohol, the light alcohol enters a light alcohol primary preheater and a light alcohol secondary preheater and then is gradually heated, and finally enters the middle part of a primary-effect evaporation recovery tower to separate the anhydrous alcohol from the water, the anhydrous alcohol is evaporated and recovered, and the water enters the bottom of the primary-effect evaporation recovery tower and enters a reboiler through a water return pipe to be heated to 160 ℃ for recycling;
the water vapor containing a small amount of anhydrous alcohol separated by the triple-effect membrane component enters a triple-effect analysis condenser to be changed into the light alcohol, the light alcohol enters a light alcohol primary preheater and a light alcohol secondary preheater and then is gradually heated, finally the light alcohol enters the middle part of the single-effect evaporation recovery tower to separate the anhydrous alcohol and the water from the light alcohol, the anhydrous alcohol is evaporated and recovered, and the water enters the bottom of the single-effect evaporation recovery tower and enters a reboiler through a water return pipe to be heated to 160 ℃ for recycling.
Preferably, in the step (1), the concentration of the raw material alcohol is 95% (v/v); the first raw material alcohol accounts for 42% of the raw material alcohol by mass, the second raw material alcohol accounts for 33% of the raw material alcohol by mass, and the third raw material alcohol accounts for 25% of the raw material alcohol by mass.
Preferably, in the step (2), the first-effect membrane assembly, the second-effect membrane assembly and the third-effect membrane assembly are all a plurality of shell-and-tube membrane structures connected in series, each shell-and-tube membrane structure comprises an outer shell and an inner tube located inside the outer shell, and the inner tube comprises a ceramic tube and a molecular sieve membrane covering the outer surface of the ceramic tube.
Preferably, the reboiler, the second-effect evaporator and the third-effect evaporator are all in a shell-and-tube structure and comprise a shell and an inner tube positioned inside the shell; the raw material preheater, the first-effect feeding first-stage preheater, the first-effect feeding second-stage preheater, the second-effect feeding first-stage preheater, the second-effect feeding second-stage preheater, the third-effect feeding preheater, the light alcohol first-stage preheater and the light alcohol second-stage preheater are all spiral plate type heat exchangers.
The tube pass of the reboiler is internally communicated with water flowing out of the single-effect evaporation recovery tower, the shell pass is internally communicated with steam, and the steam heats the water in the tube pass and is changed into condensed water.
The shell pass of the second-effect evaporator is internally filled with first absolute alcohol steam, the tube pass is internally filled with raw material alcohol, and the raw material alcohol is changed into alcohol steam by the heat of the first absolute alcohol;
second absolute alcohol steam is introduced into the shell pass of the triple-effect evaporator, raw alcohol is introduced into the tube pass, and the raw alcohol is changed into alcohol steam by the heat of the second absolute alcohol;
the raw material preheater, the first-effect feeding first-stage preheater, the first-effect feeding second-stage preheater, the second-effect feeding first-stage preheater, the second-effect feeding second-stage preheater, the third-effect feeding preheater, the light alcohol first-stage preheater and the light alcohol second-stage preheater are all spiral plate heat exchangers. Because each preheater and the pipeline work above the saturation pressure, the raw material alcohol and water (water heated by the reboiler) are still in liquid form although the temperature is higher than 100 ℃ under the pressure action.
The raw material alcohol and the third anhydrous alcohol steam in the raw material preheater exchange heat (preheat to 80 ℃);
the heat exchange (preheating to 115 ℃) of the condensed liquid of the raw material alcohol and the first anhydrous alcohol steam is carried out in the first-effect feeding first-stage preheater;
the heat exchange (preheating to 125 ℃) between the raw material alcohol and the condensed water flowing out from the reboiler is carried out in the primary-effect feeding secondary preheater;
the heat exchange (preheating to 108 ℃) of condensate after condensation of the raw material alcohol and the second anhydrous alcohol steam is carried out in the two-effect feeding primary preheater;
the heat exchange (preheating to 113 ℃) between the raw material alcohol and the condensed water flowing out from the reboiler is carried out in the two-effect feeding secondary preheater;
the heat exchange (preheating to 100 ℃) between the raw material alcohol and the condensed water flowing out of the reboiler is carried out in the triple-effect feeding preheater;
heat exchange is carried out between the weak alcohol and condensate after the first anhydrous alcohol steam is condensed in the weak alcohol primary preheater;
the inside of the weak alcohol secondary preheater exchanges heat between weak alcohol and waste water discharged from the bottom of the first-effect evaporation recovery tower (preheated to 153 ℃).
The utility model has the advantages that:
1. the utility model discloses a method compares with single-effect pervaporation membrane separation technology, adopts triple effect thermal coupling dehydration technology, utilizes the anhydrous alcohol steam of previous effect as the heat source of the raw materials alcohol evaporimeter of next effect, has realized thermal reuse, and ton anhydrous alcohol consumes vapour and is no longer than 0.2 ton, compares with single-effect pervaporation membrane separation dehydration technology, and is energy-conserving more than 55%.
2. The utility model discloses a method compares with single-effect pervaporation membrane separation technique, and the purification can not retrieved in addition by abandonment or the light alcohol of dehydration production, can accomplish the purification of light alcohol under the condition of not additionally consuming energy.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a flow chart of a triple-effect membrane separation dehydration energy-saving process for preparing anhydrous alcohol.
In the figure: 1. a raw material preheater, 2, a first-effect evaporation recovery tower, 3, a second-effect evaporator, 4, a third-effect evaporator, 5, a finished product cooler, 6, a reboiler, 7, a first-effect feeding first-stage preheater, 8, a second-effect feeding first-stage preheater, 9, a first-effect feeding second-stage preheater, 10, a second-effect feeding second-stage preheater, 11, a third-effect feeding preheater, 12, a fresh alcohol first-stage preheater, 13, a fresh alcohol second-stage preheater, 14, a first-effect superheater, 15, a first-effect membrane module, 16, a first-effect desorption condenser, 17, a second-effect superheater, 18, a second-effect membrane module, 19, a second-effect desorption condenser, 20, a third-effect superheater, 21, a third-effect membrane module, 22, a third-effect desorption condenser, 23, a third-effect condenser, 24, a first reboiler pipe, 25, a water return pipe, 26, a second reboiler pipe, 27, a first anhydrous alcohol steam pipe, 28, 29. a third anhydrous alcohol steam pipe, 30, a first alcohol feeding pipe, 31, a second alcohol feeding pipe, 32, a third alcohol feeding pipe, 33, a first alcohol discharging pipe, 34, a second alcohol discharging pipe.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the disclosure. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs.
In the description of the present invention, it should be noted that the terms "upper", "lower", "inner", "outer", etc. indicate the orientation or positional relationship that is commonly expressed, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed in a specific orientation, and be operated, and therefore should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
As background technology, currently, alcohol dehydration adopts pervaporation membrane separation technology with lowest energy consumption, and the pervaporation membrane separation technology is that raw material alcohol is firstly sent into a distillation tower for distillation, then sent into a one-effect membrane component for purification to obtain anhydrous alcohol steam, and the anhydrous alcohol is obtained after cooling. However, in the process, a lot of heat is used only once, and the purified light alcohol is generally discarded or additionally recycled, so that not only is heat wasted, but also extra energy is consumed for recycling the light alcohol.
Based on this, the utility model provides a triple effect membrane separation dehydration economizer for preparing anhydrous alcohol carries out the heat multiple use that distills the production with raw materials alcohol, can also not consume unnecessary energy and just separate the recovery purification with light alcohol.
The utility model discloses a triple-effect membrane separation dehydration economizer for preparing anhydrous alcohol, including raw materials pre-heater 1, reboiler 6, finished product cooler 5, first alcohol evaporation dewatering system, second alcohol evaporation dewatering system and third alcohol evaporation dewatering system; the raw material preheater 1 is connected with a first alcohol evaporation dehydration system through a first alcohol feeding pipe 30, the raw material preheater 1 is connected with a second alcohol evaporation dehydration system through a second alcohol feeding pipe 31, and the raw material preheater 1 is connected with a third alcohol evaporation dehydration system through a third alcohol feeding pipe 32; the reboiler 6 is connected to a first alcohol evaporation and dehydration system through a first reboiler pipe 24, and the first alcohol evaporation and dehydration system is connected to a second alcohol evaporation and dehydration system through a first anhydrous alcohol steam pipe 27; the second alcohol evaporation dehydration system is connected with a third alcohol evaporation dehydration system through a second anhydrous alcohol steam pipe 28; the second alcohol evaporation dehydration system is sequentially connected with the first alcohol evaporation dehydration system and the finished product cooler 5 through a first alcohol discharge pipe 33, the third alcohol evaporation dehydration system is sequentially connected with the second alcohol evaporation dehydration system and the finished product cooler 5 through a second alcohol discharge pipe 34, and the third alcohol evaporation dehydration system is connected with the finished product cooler 5 through a third anhydrous alcohol steam pipe 29;
the first alcohol evaporation dehydration system comprises a first-effect evaporation recovery tower 2 and a first-effect membrane assembly 15; the upper part of the primary-effect evaporation recovery tower 2 is sequentially connected with a primary-effect feeding secondary preheater 9, a primary-effect feeding primary preheater 7 and a raw material preheater 1 through a first alcohol feeding pipe 30, and the top of the primary-effect evaporation recovery tower 2 is connected with a primary-effect membrane assembly 15; the bottom of the primary evaporation recovery tower 2 is connected with a light alcohol secondary preheater 13;
the second alcohol evaporation dehydration system comprises a double-effect evaporator 3 and a double-effect membrane assembly 18; the middle part of the second-effect evaporator 3 is sequentially connected with a second-effect feeding secondary preheater 10, a second-effect feeding primary preheater 8 and a raw material preheater 1 through a second alcohol feeding pipe 31, and the top part of the second-effect evaporator 3 is connected with a second-effect membrane assembly 18;
the third alcohol evaporation dehydration system comprises a triple-effect evaporator 4 and a triple-effect membrane assembly 21; the middle part of the triple-effect evaporator 4 is sequentially connected with a triple-effect feed preheater 11 and a raw material preheater 1 through a third alcohol feed pipe 32, and the top part of the triple-effect evaporator 4 is connected with a triple-effect membrane assembly 21.
Further, the top of the primary evaporation recovery tower 2 is connected with a primary membrane module 15 through a primary superheater 14; the top of the secondary-effect evaporator 3 is connected with a secondary-effect membrane assembly 18 through a secondary-effect superheater 17; the top of the triple-effect evaporator 4 is connected with a triple-effect membrane assembly 21 through a triple-effect superheater 20.
Further, the first-effect membrane assembly 15 is connected with the upper part of the second-effect evaporator 3 through a first anhydrous alcohol steam pipe 27; the secondary-effect membrane assembly 18 is connected with the upper part of the triple-effect evaporator 4 through a second anhydrous alcohol steam pipe 28; the triple-effect membrane module 21 is sequentially connected with a raw material preheater 1, a triple-effect condenser 23 and a finished product cooler 5 through a third anhydrous alcohol steam pipe 29.
Further, the lower part of the second-effect evaporator 3 is sequentially connected with a first-effect feeding first-stage preheater 7, a light alcohol first-stage preheater 12 and a finished product cooler 5 through a first alcohol discharge pipe 33; the lower part of the triple-effect evaporator 4 is sequentially connected with a double-effect feeding primary preheater 8 and a finished product cooler 5 through a second alcohol discharging pipe 34.
Further, the first-effect membrane assembly 15 is sequentially connected with a first-effect desorption condenser 16, a first-stage light alcohol preheater 12 and a second-stage light alcohol preheater 13 through pipelines, and then is connected with the middle part of the first-effect evaporation recovery tower 2; the double-effect membrane assembly 18 is connected with the primary light alcohol preheater 12 through a double-effect desorption condenser 19; the triple-effect membrane component 21 is connected with the primary alcohol preheater 12 through a triple-effect desorption condenser 22.
Further, the reboiler 6 and the first-effect evaporation recovery tower 2 are respectively connected through a first reboiler pipe 24 and a water return pipe 25, and the reboiler 6 is sequentially connected with a first-effect feeding secondary preheater 9, a second-effect feeding secondary preheater 10 and a third-effect feeding preheater 11 through a second reboiler pipe 26.
In order to make the technical solutions of the present application more clearly understood by those skilled in the art, the technical solutions of the present application will be described in detail below with reference to specific embodiments. If the experimental conditions not specified in the examples are specified, the conditions are generally conventional or recommended by the reagent company; reagents, consumables, and the like used in the following examples are commercially available unless otherwise specified.
Examples
The raw material alcohol of 95% (v/v) is preheated by a raw material preheater 1 and then divided into three parts:
(1) raw material alcohol accounting for 42 percent of the mass fraction enters a primary-effect feeding primary preheater 7 through a first alcohol feeding pipe 30 to be preheated to 115 ℃, then enters a primary-effect feeding secondary preheater 9 to be heated to 125 ℃, and finally enters the upper part of a primary-effect evaporation recovery tower 2 to be distilled. The water at the bottom of the first-effect evaporation recovery tower 2 enters the reboiler 6 through the water return pipe 25, the steam enters the reboiler 6 to heat the water to 160 ℃, the steam pressure is 0.6MPa, the heated hot water enters the first-effect evaporation recovery tower 2 through the first reboiler pipe 24, the temperature at the bottom of the first-effect evaporation recovery tower 2 is 153 ℃, heat is provided for distillation of raw material alcohol, and the raw material alcohol is changed into alcohol steam. Condensed water in the shell pass of the reboiler 6 sequentially enters the primary-effect feeding secondary preheater 9, the secondary-effect feeding secondary preheater 10 and the tertiary-effect feeding preheater 11 through a second reboiler pipeline 26 to provide heat, and hot water after providing heat returns to a boiler room and is changed into steam to continue to heat the reboiler 6. The alcohol vapor enters the first-effect superheater 14 for further heating and then enters the first-effect membrane assembly 15 for dehydration and purification, the alcohol vapor enters the shell side of the first-effect membrane assembly 15, under the pressure of 0.5MPa, through the Dalton partial pressure law, the water vapor in the alcohol vapor permeates the inner tube with the molecular sieve membrane, meanwhile, a small amount of alcohol vapor is carried by the water vapor to permeate the inner tube, and the liquid in the inner tube becomes the weak alcohol vapor. The weak alcohol steam is cooled into weak alcohol through a first-effect desorption condenser 16, the weak alcohol sequentially enters a weak alcohol first-stage preheater 12 and a weak alcohol second-stage preheater 13 for preheating, and finally enters the middle part of a first-effect evaporation recovery tower 2, the weak alcohol is heated, and the separated alcohol steam moves towards the top of the tower and is converged with raw material alcohol steam on the upper part of the tower to continue to be dehydrated and purified in the next step. The water separated from the light alcohol moves to the bottom of the single-effect evaporation recovery tower 2, enters the reboiler 6 for heating through the water return pipe 25, and returns to the bottom of the tower through the first reboiler pipe 24 for continuously providing heat. The waste water at the bottom of the tower is discharged after passing through the weak alcohol secondary preheater 13 and provides heat for the weak alcohol secondary preheater 13. Purifying the first effect membrane assembly 15 to obtain first anhydrous alcohol steam, allowing the first anhydrous alcohol steam to enter the upper part of the second effect evaporator 3 and move downwards to provide distillation heat for the second effect evaporator 3 so as to maintain the temperature of the second effect evaporator 3 at 118 ℃, and then allowing the first anhydrous alcohol steam to flow out of the lower part of the second effect evaporator 3 and enter the first effect feeding first-stage preheater 7 through a first alcohol discharge pipe 33 so as to provide heat for the first effect feeding first-stage preheater 7, so that the temperature of the first effect feeding first-stage preheater 7 is maintained at; then enters a primary preheater 12 of the light alcohol to provide heat for the light alcohol, and finally enters a finished product cooler 5 to be cooled into finished product anhydrous ethanol.
(2) Raw material alcohol accounting for 33 percent of mass fraction enters a secondary-effect feeding primary preheater 8 through a second alcohol feeding pipe 31 to be preheated to 108 ℃, then enters a secondary-effect feeding preheater 10, finally enters a secondary-effect evaporator 3 to be distilled into alcohol steam, the alcohol steam enters a secondary-effect superheater 17 to be further heated, and then enters a secondary-effect membrane assembly 18 to be dehydrated and purified, the alcohol steam enters a shell side of the secondary-effect membrane assembly 18, under the pressure of 0.5MPa, through the Dalton partial pressure law, the water steam in the alcohol steam permeates an inner pipe with a molecular sieve membrane, meanwhile, a small amount of alcohol steam is carried by the water steam to permeate the inner pipe, and the liquid in the inner pipe becomes light alcohol steam. The weak alcohol steam is cooled into weak alcohol through a double-effect desorption condenser 19, the weak alcohol sequentially enters a weak alcohol primary preheater 12 and a weak alcohol secondary preheater 13 for preheating, and finally enters the middle part of the primary-effect evaporation recovery tower 2, the weak alcohol is heated, and the separated alcohol steam moves towards the top of the tower and is converged with the raw material alcohol steam on the upper part of the tower to continue to be dehydrated and purified in the next step. The water separated from the light alcohol moves to the bottom of the single-effect evaporation recovery tower 2, enters the reboiler 6 for heating through the water return pipe 25, and returns to the bottom of the tower through the first reboiler pipe 24 for continuously providing heat. The waste water at the bottom of the tower is discharged after passing through a weak alcohol secondary preheater 13. Purifying the secondary-effect membrane assembly 18 to obtain second anhydrous alcohol steam, feeding the second anhydrous alcohol steam into the upper part of the triple-effect evaporator 4 to move downwards to provide distillation heat for the triple-effect evaporator 4 so as to maintain the temperature of the triple-effect evaporator 4 at 112 ℃, and then feeding the second anhydrous alcohol steam into the secondary-effect feeding primary preheater 8 from the lower part of the triple-effect evaporator 4 through a second alcohol discharge pipe 34 so as to provide heat for the secondary-effect feeding primary preheater 8, so that the temperature of the secondary-effect feeding primary preheater 8 is maintained at 108 ℃; finally, the mixture enters a finished product cooler 5 to be cooled into finished product absolute ethyl alcohol.
(3) Raw material alcohol accounting for 25% of mass fraction enters a triple-effect feed preheater 11 through a third alcohol feed pipe 32 to be preheated to 100 ℃, then enters a triple-effect evaporator 4 to be distilled into alcohol steam, the alcohol steam enters a triple-effect superheater 20 to be further heated and then enters a triple-effect membrane assembly 21 to be dehydrated and purified, the alcohol steam enters a shell side of the triple-effect membrane assembly 21, under the pressure of 0.5MPa, through a Dalton partial pressure law, water vapor in the alcohol steam permeates an inner pipe with a molecular sieve membrane, meanwhile, a small amount of alcohol steam is carried by the water vapor to permeate the inner pipe, and liquid in the inner pipe becomes light alcohol steam. The weak alcohol steam is cooled into weak alcohol through a triple effect desorption condenser 22, the weak alcohol sequentially enters a weak alcohol primary preheater 12 and a weak alcohol secondary preheater 13 for preheating, and finally enters the middle part of a single effect evaporation recovery tower 2, the weak alcohol is heated, and the separated alcohol steam moves to the top of the tower to be converged with the raw material alcohol steam on the upper part of the tower to continue to be dehydrated and purified in the next step. The water separated from the light alcohol moves to the bottom of the single-effect evaporation recovery tower 2, enters the reboiler 6 for heating through the water return pipe 25, and returns to the bottom of the tower through the first reboiler pipe 24 for continuously providing heat. The waste water at the bottom of the tower is discharged after passing through a weak alcohol secondary preheater 13. And purifying the triple-effect membrane assembly 21 to obtain third anhydrous alcohol steam, feeding the third anhydrous alcohol steam into the raw material preheater 1 through a third anhydrous alcohol steam pipeline 29 to maintain the temperature of the raw material preheater 1 at 80 ℃, condensing the third anhydrous alcohol steam through a triple-effect condenser 23, and finally feeding the third anhydrous alcohol steam into a finished product cooler 5 to be cooled to obtain a finished product anhydrous alcohol.
Table 1 shows the steam energy consumption of the four dehydration techniques mentioned in the background and the steam energy consumption of the examples.
TABLE 1 steam energy consumption per ton of absolute alcohol produced
The above description is only a preferred embodiment of the present application and is not intended to limit the present application, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, improvement and the like made within the spirit and principle of the present application shall be included in the protection scope of the present application.
Claims (6)
1. The triple-effect membrane separation dehydration energy-saving device for preparing the anhydrous alcohol is characterized by comprising a raw material preheater; the raw material preheater is connected with a first alcohol evaporation dehydration system through a first alcohol feeding pipe, the raw material preheater is connected with a second alcohol evaporation dehydration system through a second alcohol feeding pipe, and the raw material preheater is connected with a third alcohol evaporation dehydration system through a third alcohol feeding pipe; the reboiler is connected with a first alcohol evaporation and dehydration system through a first reboiler pipe, and the first alcohol evaporation and dehydration system is connected with a second alcohol evaporation and dehydration system through a first anhydrous alcohol steam pipe; the second alcohol evaporation dehydration system is connected with the third alcohol evaporation dehydration system through a second anhydrous alcohol steam pipe; the second alcohol evaporation dehydration system is sequentially connected with the first alcohol evaporation dehydration system and the finished product cooler through a first alcohol discharge pipe, the third alcohol evaporation dehydration system is sequentially connected with the second alcohol evaporation dehydration system and the finished product cooler through a second alcohol discharge pipe, and the third alcohol evaporation dehydration system is connected with the finished product cooler through a third anhydrous alcohol steam pipe;
the first alcohol evaporation dehydration system comprises a first-effect evaporation recovery tower and a first-effect membrane assembly; the upper part of the primary-effect evaporation recovery tower is sequentially connected with a primary-effect feeding secondary preheater, a primary-effect feeding primary preheater and a raw material preheater through a first alcohol feeding pipe, and the top of the primary-effect evaporation recovery tower is connected with a primary-effect membrane assembly; the bottom of the primary evaporation recovery tower is connected with a light wine secondary preheater;
the second alcohol evaporation dehydration system comprises a double-effect evaporator and a double-effect membrane component; the bottom of the second-effect evaporator is sequentially connected with a second-effect feeding secondary preheater, a second-effect feeding primary preheater and a raw material preheater through a second alcohol feeding pipe, and the top of the second-effect evaporator is connected with a second-effect membrane assembly;
the third alcohol evaporation dehydration system comprises a triple-effect evaporator and a triple-effect membrane assembly; the bottom of the triple-effect evaporator is sequentially connected with the triple-effect feed preheater and the raw material preheater through a third alcohol feed pipe, and the top of the triple-effect evaporator is connected with the triple-effect membrane assembly.
2. The apparatus according to claim 1, wherein the top of the primary evaporation recovery tower and the primary membrane module are connected through a primary superheater; the top of the double-effect evaporator is connected with the double-effect membrane component through a double-effect superheater; the top of the triple-effect evaporator is connected with the triple-effect membrane component through a triple-effect superheater.
3. The apparatus of claim 1, wherein the primary membrane module is connected to the upper part of the secondary evaporator by a first anhydrous alcohol steam pipe; the second-effect membrane assembly is connected with the upper part of the third-effect evaporator through a second anhydrous alcohol steam pipe; the triple-effect membrane assembly is sequentially connected with the raw material preheater, the triple-effect condenser and the finished product cooler through a third absolute alcohol pipe.
4. The apparatus of claim 1, wherein the lower portion of the dual-effect evaporator is connected to a primary single-effect feed preheater, a primary weak liquor preheater and a final product cooler in sequence through a first alcohol outlet pipe; the lower part of the triple-effect evaporator is sequentially connected with a double-effect feeding primary preheater and a finished product cooler through a second alcohol discharging pipe.
5. The device according to claim 4, wherein the primary-effect membrane assembly is sequentially connected with a primary-effect desorption condenser, a primary light wine preheater and a secondary light wine preheater through pipelines and then connected with the middle part of the primary-effect evaporation recovery tower; the double-effect membrane component is connected with the light wine primary preheater through a double-effect analysis condenser; the triple-effect membrane component is connected with the light wine primary preheater through a triple-effect resolution condenser.
6. The apparatus of claim 1, wherein the reboiler is connected to the primary evaporative recovery tower via a first reboiler pipe and a water return pipe, respectively, and the reboiler is connected to the primary feed secondary preheater, the secondary feed secondary preheater, and the tertiary feed preheater in this order via a second reboiler pipe.
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| WO2023193744A1 (en) * | 2022-04-08 | 2023-10-12 | 浙江汇甬新材料有限公司 | Membrane separation and purification device and method |
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Address after: 271600 hi tech Industrial Development Zone, Tai'an, Shandong, Feicheng Patentee after: Shandong Jinta Machinery Group Co., Ltd Address before: 271608 71 Kang Hui Street, hi tech Industrial Development Zone, Feicheng, Tai'an, Shandong Patentee before: FEICHENG PYRAMID MACHINERY Co.,Ltd. |