Co-production method of common-grade wine and superior-grade wine

Abstract

The invention relates to the field of ethanol production, and discloses a common-grade wine and superior-grade wine co-production method, which comprises: S1, carrying out primary rectification on a fermentation mash to obtain a crude wine; s2, washing the crude wine obtained in S1 with water to obtain light wine; s3, carrying out first rectification on at least one part of the light wine obtained in S2 to obtain purified concentrated liquid; s4, removing methanol from at least one part of the purified and concentrated liquid obtained in S3 to obtain a superior wine product; s5, carrying out second rectification on at least one part of the light wine obtained in S2 to obtain a common-grade wine product; wherein the rectification temperatures of the primary rectification, the second rectification and the first rectification are gradually increased in sequence. By adopting the method disclosed by the invention, high-quality common-grade wine and superior-grade wine products can be produced at the same time, the energy consumption is low, and the product yield is high.

Description

Technical Field

[0001] This invention relates to the field of ethanol production, specifically to a method for the co-production of ordinary and premium grade liquor. Background Technology

[0002] Alcohol, as an important solvent and chemical raw material, is widely used in the chemical industry and medical and health care sectors. It is also a fundamental raw material for the beverage industry and a convenient and relatively clean liquid fuel. Its production methods include fermentation using plant-based materials and chemical synthesis using petroleum-based materials. Before the 1950s, alcohol was mainly produced through fermentation. Although the chemical synthesis method was simpler, it lacked large-scale industrial production due to limitations in raw material sources. Fermentation-based alcohol production is currently the most fundamental industry in the bio-industry, and its production technology is continuously advancing with the development of bioengineering technology.

[0003] Edible alcohol, also known as edible brewed alcohol, is a hydrous alcohol produced from grains, potatoes, molasses, or other edible crops through fermentation, distillation, and refining. It is used in the food industry. Edible alcohol has become a widely used food additive globally. In recent years, the domestic edible alcohol market has seen continuous growth in both size and consumption, with strong policy support bringing positive impacts to the market.

[0004] Edible alcohol includes both regular and premium spirits. A typical premium spirits distillation process uses a 6-tower differential pressure distillation process. The distillation unit includes a crude distillation tower, a crude auxiliary distillation tower, a water washing tower, a methanol distillation tower, a refining tower, and a recovery tower. This process is complex and energy-intensive, consuming approximately 2.5 tons of steam per ton of product to produce premium spirits. Currently, there is no specifically designed distillation process for regular spirits. Generally, by adjusting process parameters based on the 6-tower system for premium spirits, regular spirits can be obtained. This results in long, complex distillation processes, high investment, and high energy consumption in co-production projects of both regular and premium spirits.

[0005] Therefore, there is an urgent need to provide a process that can simultaneously produce premium and regular wines, and that is simple and energy-efficient. Summary of the Invention

[0006] The purpose of this invention is to overcome the problems of long process, complex technology, high investment and high energy consumption in the co-production of premium and ordinary wines in the existing technology, and to provide a method for co-producing ordinary and premium wines. This method has a simple process, low energy consumption, greatly reduces production costs, and has flexible product solutions, and can simultaneously produce ordinary and premium wine products that meet national standards.

[0007] To achieve the above objectives, the present invention provides a method for the joint production of ordinary-grade and premium-grade wines, the method comprising:

[0008] S1. The fermented mash is subjected to primary distillation to obtain crude liquor;

[0009] S2. Wash the crude wine obtained in S1 with water to obtain a light wine;

[0010] S3. At least a portion of the light wine obtained in S2 is subjected to a first distillation to obtain a purified and concentrated liquid;

[0011] S4. Remove methanol from the purified and concentrated liquid obtained in S3 to obtain a premium wine product.

[0012] S5. At least a portion of the light liquor obtained in S2 is subjected to a second distillation to obtain a standard grade liquor product;

[0013] The distillation temperature of the second distillation is 30-50°C higher than that of the primary distillation, and the distillation temperature of the first distillation is 30-45°C higher than that of the second distillation.

[0014] Through the above technical solution, the present invention achieves at least the following beneficial technical effects:

[0015] (1) The method of the present invention can simultaneously produce high-quality ordinary-grade wine and premium-grade wine products.

[0016] (2) The process of producing ordinary and superior wines using the method of the present invention is simple, has low energy consumption, and reduces production costs. In the preferred embodiment, compared with the traditional process, the method of the present invention saves up to 20% in energy consumption.

[0017] (3) The method of the present invention produces high yields of ordinary and superior wines. In the preferred embodiment, the product yield is over 99%. Attached Figure Description

[0018] Figure 1 This is a flowchart of a preferred embodiment of the present invention for the preparation of ordinary grade wine and superior grade wine.

[0019] Figure 2 This is a flowchart of the production of premium / standard wine using the traditional 6-tower process in Comparative Example 1.

[0020] Explanation of reference numerals in the attached figures

[0021] T1 Crude Distillation Column, T2 Water Washing Column, T3 First Rectifying Column

[0022] T4 Second Distillation Column, T5 Methanol Column Detailed Implementation

[0023] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0024] This invention provides a method for the joint production of ordinary and premium grade wines, the method comprising:

[0025] S1. The fermented mash is subjected to primary distillation to obtain crude liquor;

[0026] S2. Wash the crude wine obtained in S1 with water to obtain a light wine;

[0027] S3. At least a portion of the light wine obtained in S2 is subjected to a first distillation to obtain a purified and concentrated liquid;

[0028] S4. Remove methanol from the purified and concentrated liquid obtained in S3 to obtain a premium wine product.

[0029] S5. At least a portion of the light liquor obtained in S2 is subjected to a second distillation to obtain a standard grade liquor product;

[0030] The distillation temperature of the second distillation is 30-50°C higher than that of the primary distillation, and the distillation temperature of the first distillation is 30-45°C higher than that of the second distillation.

[0031] In this invention, primary distillation, first distillation, and second distillation are carried out in a crude distillation column, a first distillation column, and a second distillation column, respectively. The distillation temperature in this invention includes the top temperature or the bottom temperature, and the distillation pressure includes the top pressure or the bottom pressure.

[0032] According to some embodiments of the present invention, in S1, the primary distillation method includes: performing primary distillation on the fermentation mash in a crude distillation column to obtain the top gas of the crude distillation column, the bottom material of the crude distillation column, and crude liquor.

[0033] To further improve the removal efficiency of CO2 and light aldehydes, the primary distillation conditions preferably include: a top pressure of 25 kPa to 35 kPa and a top temperature of 45-70°C; a bottom pressure of 35 kPa to 60 kPa and a bottom temperature of 75-90°C; and a reflux ratio of 0.3-0.7.

[0034] To further improve the removal efficiency of fusel oil and n-propanol, preferably, in S2, when performing the water washing, the amount of water used is such that the weight ratio of water to crude wine is (1-4):1, preferably (1-2.5):1.

[0035] According to a preferred embodiment of the present invention, in step S2, the water washing method includes: washing the crude wine in a water washing tower to remove fusel oil and n-propanol from the crude wine, thereby obtaining a diluted wine. When the concentration of ethanol at the top of the water washing tower is about 40 wt%, fusel oil and n-propanol accumulate in large quantities at the top of the tower. Washing with the water washing tower removes fusel oil and n-propanol, ensuring that the n-propanol content in the product meets the standard.

[0036] Preferably, the washing conditions include: a tower top pressure of 100 kPa to 120 kPa and a tower top temperature of 85-92°C; a tower bottom pressure of 110 kPa to 140 kPa and a tower bottom temperature of 90-100°C; and a reflux ratio of 1-3.

[0037] Preferably, the ethanol content in the diluted wine after washing is 10-20 wt%.

[0038] According to a preferred embodiment of the present invention, in step S3, the first distillation method includes: in a first distillation column, purifying and concentrating at least a portion of the light wine obtained in step S2 to obtain purified and concentrated liquid, fusel oil-containing material and column bottom wastewater.

[0039] To further improve the purification and concentration effect of the diluted wine after washing, preferably, the conditions for the first distillation include: a top pressure of 400 kPa to 450 kPa and a top temperature of 130-140°C; a bottom pressure of 420 kPa to 520 kPa and a bottom temperature of 150-160°C; and a reflux ratio of 3-8.

[0040] In this invention, methanol removal is carried out in a methanol tower. Methanol has the characteristic that when the alcohol concentration is greater than 40 wt%, the rectification coefficient is greater than 1, and the higher the alcohol concentration, the greater the rectification coefficient. Therefore, the efficiency of separating methanol from alcohol at high concentrations is higher. After passing through the methanol tower, the methanol content in the alcohol produced from the methanol tower can reach 30-50 ppm. The bottom material of the methanol tower is collected as a premium-grade alcoholic beverage.

[0041] According to a preferred embodiment of the present invention, in step S4, the method for removing methanol includes: removing methanol from the purified and concentrated liquid obtained in step S3 in a methanol tower to obtain a premium wine product.

[0042] To further improve the methanol removal efficiency, preferably, the methanol removal conditions include: a top pressure of 50 kPa to 70 kPa and a top temperature of 60-70°C; a bottom pressure of 75 kPa to 85 kPa and a bottom temperature of 68-80°C; and a reflux ratio of 1-3.

[0043] According to a preferred embodiment of the present invention, in step S5, the second distillation method includes: in a second distillation column, separating at least a portion of the light wine obtained in step S2 into ethanol and water to obtain a standard-grade wine product, fusel oil-containing material, and column bottom wastewater.

[0044] According to a preferred embodiment of the present invention, based on the total mass of the light wine, in S3, the flow rate of the light wine for the first distillation is 40-50 wt%; in S5, the flow rate of the light wine for the second distillation is 50-60 wt%.

[0045] According to a preferred embodiment of the present invention, the conditions for the second distillation include: a top pressure of 160 kPa to 200 kPa and a top temperature of 105-115°C; a bottom pressure of 200 kPa to 300 kPa and a bottom temperature of 120-130°C; and a reflux ratio of 2-5.

[0046] According to a preferred embodiment of the present invention, combined with Figure 1 This describes a method for the joint production of standard and premium wines, the method comprising:

[0047] S1. The fermentation mash is introduced into the crude distillation column T1 for primary distillation. The top gas of the crude distillation column T1 is produced, and the crude wine and the bottom feed of the crude distillation column T1 are collected from the side stream. The top gas (mainly including CO2 and light hydrocarbons such as aldehydes) is discharged from the top of the crude distillation column T1 and enters the reflux tank. A portion of the reflux tank is returned as reflux to the crude distillation column T1.

[0048] S2. The crude liquor drawn from the side stream of the crude distillation tower T1 is introduced into the washing tower T2 for washing. In the washing tower T2, fusel oil (which is drawn from the top of the washing tower T2 as an industrial liquor by-product) and n-propanol are removed from the crude liquor. The washed light liquor is obtained from the bottom of the washing tower T2.

[0049] S3. Pump the washed light wine portion into the first distillation column T3. After purification and concentration in the first distillation column T3, the material containing fusel oil is collected from the side stream of the first distillation column T3 (output as a by-product). Wastewater is produced in the bottom of the column, and a portion of the purified and concentrated liquid is collected from the top of the column.

[0050] S4. The purified and concentrated liquid produced from the top of the first distillation column T3 enters the methanol column T5. After further removal of methanol in the methanol column T5, the premium wine product is collected from the bottom of the methanol column T5.

[0051] S5. The diluted liquor obtained from S2 after washing is pumped into the second distillation column T4. Ethanol and water are separated in the second distillation column T4. The ordinary grade liquor product is collected from the top of the second distillation column T4, and the wastewater is collected from the bottom of the column (the wastewater is returned to the slurry preparation system for recycling). The material containing fusel oil is collected from the side stream of the column and enters the fusel oil washing tank. The fusel oil is collected as a by-product and output.

[0052] The overhead gas from the first distillation column T3 serves as a heat source for the reboiler of the second distillation column T4; the overhead gas from the second distillation column T4 serves as a heat source for the reboiler of the water washing column T2 and the crude distillation column T1, respectively; the overhead gas from the water washing column T2 serves as a heat source for the methanol column T5; and the reboiler of the first distillation column uses fresh steam as a heat source. Fresh steam distillation is an optimized combination of four-effect and three-effect heat exchangers, and it eliminates the need for separate crude auxiliary columns and recovery columns, resulting in lower energy consumption than traditional three-effect heat exchange processes in distillation.

[0053] According to a particularly preferred embodiment of the present invention, a method for the co-production of ordinary-grade and premium-grade wines is provided, the method comprising:

[0054] S1. The fermentation mash is introduced into the crude distillation column for primary distillation. The conditions for primary distillation include: the top temperature of the crude distillation column is 50-55℃, the top pressure is 30-33kPa, the bottom temperature is 80-83℃, the bottom pressure is 50-55kPa, and the reflux ratio is 0.4-0.5. The top gas is produced from the top of the crude distillation column, and the crude liquor and the bottom feed of the crude distillation column are collected from the side stream. The top gas (mainly including CO2 and light hydrocarbons such as aldehydes) is discharged from the top of the crude distillation column into the reflux tank, and a portion of the reflux from the reflux tank is returned as reflux to the crude distillation column.

[0055] S2. The crude liquor collected from the reflux tank of the crude distillation column is introduced into the washing column for washing. The mass ratio of water to crude liquor is (1-1.5):1. The washing conditions include: the top temperature of the column is 86-87℃, the top pressure of the column is 100-120kPa, the bottom temperature of the column is 90-93℃, the bottom pressure of the column is 120-130kPa, and the reflux ratio is 1-3. In the washing column, fusel oil (which is collected from the top of the washing column as an industrial liquor by-product) and n-propanol are removed from the crude liquor. The washed light liquor is obtained from the bottom of the washing column. The ethanol content of the light liquor is 10-20wt%.

[0056] S3. Pump the washed light wine portion into the first distillation column for the first distillation column. After purification and concentration, the material containing fusel oil is collected from the side stream of the first distillation column (output as a by-product). Wastewater is produced in the bottom of the column, and a portion of the purified and concentrated liquid is collected from the top of the column.

[0057] The conditions for the first distillation include: a top temperature of 135-138℃, a top pressure of 410-440 kPa, a bottom temperature of 155-158℃, a bottom pressure of 450-510 kPa, and a reflux ratio of 4-6.

[0058] S4. The purified and concentrated liquid produced from the top of the first distillation column enters the methanol column. After further removing methanol in the methanol column, the premium wine product is collected from the bottom of the methanol column.

[0059] The conditions for removing methanol include: top temperature of 65-68℃, top pressure of 55-65kPa, bottom temperature of 70-75℃, bottom pressure of 76-80kPa, and reflux ratio of 1-2.

[0060] S5. The diluted liquor obtained from S2 after washing is pumped into the second distillation column, where a second distillation is carried out (to separate ethanol and water). The ordinary grade liquor product is collected from the top of the second distillation column, and the wastewater is collected from the bottom of the column (the wastewater is returned to the slurry preparation system for recycling). The material containing fusel oil is collected from the side stream of the column and enters the fusel oil washing tank. The fusel oil is collected as a by-product and output.

[0061] The conditions for the second distillation include: a top temperature of 110-112℃, a top pressure of 165-175kPa, a bottom temperature of 122-128℃, a bottom pressure of 210-225kPa, and a reflux ratio of 2.5-4.

[0062] The present invention will be described in detail below through embodiments.

[0063] All pressures in this invention are gauge pressures.

[0064] Unless otherwise specified, the following embodiments are all conventional methods.

[0065] Unless otherwise specified, all reagents and materials used in the following examples are commercially available.

[0066] Example 1

[0067] This embodiment provides a method for preparing both standard-grade and premium-grade wines.

[0068] Using corn as raw material, it produces ordinary liquor (55,000 tons / year) and premium liquor (45,000 tons / year).

[0069] S1. The fermentation mash (ethanol content 15%V) is introduced into the crude distillation column for primary distillation. The conditions for primary distillation include: the top temperature of the crude distillation column is 53℃, the top pressure is 32kPa, the bottom temperature is 83℃, the bottom pressure is 52kPa, and the reflux ratio is 0.5. The top gas is produced from the top of the crude distillation column, and the crude liquor and the bottom feed of the crude distillation column are collected from the side stream. The top gas (mainly including CO2 and light hydrocarbons such as aldehydes) is discharged from the top of the crude distillation column into the reflux tank, and a portion of the reflux from the reflux tank is returned as reflux from the crude distillation column.

[0070] S2. The crude liquor collected from the reflux tank of the crude distillation column is introduced into the washing column for washing. The mass ratio of water to crude liquor is 1.5:1. The washing conditions include: top temperature of 87℃, top pressure of 100kPa, bottom temperature of 93℃, bottom pressure of 128kPa, and reflux ratio of 1. In the washing column, fusel oil (collected from the top of the washing column as an industrial liquor by-product) and n-propanol are removed from the crude liquor. The washed light liquor is obtained from the bottom of the washing column, and the ethanol content of the light liquor is 10wt%.

[0071] S3. Pump 55% of the diluted wine after washing into the first distillation column, and carry out the first distillation in the first distillation column. After purification and concentration, the material containing fusel oil is collected from the side stream of the first distillation column (output as a by-product). Wastewater is produced in the bottom of the column, and a portion of the purified and concentrated liquid is collected from the top of the column.

[0072] The conditions for the first distillation include: a top temperature of 136°C, a top pressure of 420 kPa, a bottom temperature of 156°C, a bottom pressure of 500 kPa, and a reflux ratio of 5.

[0073] S4. The purified and concentrated liquid (ethanol content of 95% and methanol content of 50ppm) produced from the top of the first distillation column enters the methanol column. After further removal of methanol in the methanol column, the premium wine product (methanol content of 30ppm) is collected from the bottom of the methanol column.

[0074] The conditions for removing methanol include: a top temperature of 66°C, a top pressure of 60 kPa, a bottom temperature of 70°C, a bottom pressure of 80 kPa, and a reflux ratio of 2.

[0075] S5. Pump 45% of the diluted liquor flow rate obtained from S2 into the second distillation column for second distillation (separation of ethanol and water). Collect the ordinary grade liquor product from the top of the second distillation column, collect the wastewater from the bottom of the column (the wastewater is returned to the slurry preparation system for recycling), and collect the material containing fusel oil from the side stream of the column into the fusel oil washing tank. The fusel oil is collected as a by-product and output.

[0076] The conditions for the second distillation include: a top temperature of 112°C, a top pressure of 170 kPa, a bottom temperature of 125°C, a bottom pressure of 220 kPa, and a reflux ratio of 2.5.

[0077] Example 2

[0078] This embodiment provides a method for preparing both standard-grade and premium-grade wines.

[0079] Using corn as raw material, it produces ordinary liquor (55,000 tons / year) and premium liquor (45,000 tons / year).

[0080] S1. The fermentation mash (ethanol content 15%V) is introduced into the crude distillation column for primary distillation. The conditions for primary distillation include: the top temperature of the crude distillation column is 40℃, the top pressure is 25kPa, the bottom temperature is 75℃, the bottom pressure is 35kPa, and the reflux ratio is 0.3. The top gas is produced from the top of the crude distillation column, and the crude liquor and the bottom feed of the crude distillation column are collected from the side stream. The top gas (mainly including CO2 and light hydrocarbons such as aldehydes) is discharged from the top of the crude distillation column into the reflux tank, and a portion of the reflux from the reflux tank is returned as reflux from the crude distillation column.

[0081] S2. The crude liquor collected from the reflux tank of the crude distillation column is introduced into a water washing tower for washing. The mass ratio of water to crude liquor is 2:1. The washing conditions include: top temperature of 85℃, top pressure of 100kPa, bottom temperature of 90℃, bottom pressure of 110kPa, and reflux ratio of 1. In the water washing tower, fusel oil (collected from the top of the water washing tower as an industrial liquor by-product) and n-propanol are removed from the crude liquor. The washed light liquor is obtained from the bottom of the water washing tower, and the ethanol content of the light liquor is 10wt%.

[0082] S3. Pump 55% of the diluted wine after washing into the first distillation column, and carry out the first distillation in the first distillation column. After purification and concentration, the material containing fusel oil is collected from the side stream of the first distillation column (output as a by-product). Wastewater is produced in the bottom of the column, and a portion of the purified and concentrated liquid is collected from the top of the column.

[0083] The conditions for the first distillation include: a top temperature of 130°C, a top pressure of 400 kPa, a bottom temperature of 150°C, a bottom pressure of 420 kPa, and a reflux ratio of 3.

[0084] S4. The purified and concentrated liquid (ethanol content of 95% and methanol content of 60ppm) produced from the top of the first distillation column enters the methanol column. After further removal of methanol in the methanol column, the premium wine product (methanol content of 45ppm) is collected from the bottom of the methanol column.

[0085] The conditions for removing methanol include: a top temperature of 60°C, a top pressure of 50 kPa, a bottom temperature of 68°C, a bottom pressure of 75 kPa, and a reflux ratio of 1.

[0086] S5. Pump 45% of the diluted liquor flow rate obtained from S2 into the second distillation column for second distillation (separation of ethanol and water). Collect the ordinary grade liquor product from the top of the second distillation column, collect the wastewater from the bottom of the column (the wastewater is returned to the slurry preparation system for recycling), and collect the material containing fusel oil from the side stream of the column into the fusel oil washing tank. The fusel oil is collected as a by-product and output.

[0087] The conditions for the second distillation include: a top temperature of 105°C, a top pressure of 160 kPa, a bottom temperature of 120°C, a bottom pressure of 200 kPa, and a reflux ratio of 2.

[0088] Example 3

[0089] This embodiment provides a method for preparing both standard-grade and premium-grade wines.

[0090] Using corn as raw material, it produces ordinary liquor (55,000 tons / year) and premium liquor (45,000 tons / year).

[0091] S1. The fermentation mash (ethanol content 15%V) is introduced into the crude distillation column for primary distillation. The conditions for primary distillation include: the top temperature of the crude distillation column is 70℃, the top pressure is 35kPa, the bottom temperature is 90℃, the bottom pressure is 60kPa, and the reflux ratio is 0.7. The top gas is produced from the top of the crude distillation column, and the crude liquor and the bottom feed of the crude distillation column are collected from the side stream. The top gas (mainly including CO2 and light hydrocarbons such as aldehydes) is discharged from the top of the crude distillation column into the reflux tank, and a portion of the reflux from the reflux tank is returned as reflux from the crude distillation column.

[0092] S2. The crude liquor collected from the reflux tank of the crude distillation column is introduced into the washing column for washing. The mass ratio of water to crude liquor is 3:1. The washing conditions include: top temperature of 92℃, top pressure of 120kPa, bottom temperature of 100℃, bottom pressure of 140kPa, and reflux ratio of 3. In the washing column, fusel oil (collected from the top of the washing column as an industrial liquor by-product) and n-propanol are removed from the crude liquor. The washed light liquor is obtained from the bottom of the washing column, and the ethanol content of the light liquor is 10wt%.

[0093] S3. Pump 45% of the diluted wine after washing into the first distillation column, and carry out the first distillation in the first distillation column. After purification and concentration, the material containing fusel oil is collected from the side stream of the first distillation column (output as a by-product). Wastewater is produced in the bottom of the column, and a portion of the purified and concentrated liquid is collected from the top of the column.

[0094] The conditions for the first distillation include: a top temperature of 140°C, a top pressure of 450 kPa, a bottom temperature of 160°C, a bottom pressure of 520 kPa, and a reflux ratio of 8.

[0095] S4. The purified and concentrated liquid (ethanol content of 95% and methanol content of 40ppm) produced from the top of the first distillation column enters the methanol column. After further removal of methanol in the methanol column, the premium wine product (methanol content of 20ppm) is collected from the bottom of the methanol column.

[0096] The conditions for removing methanol include: a top temperature of 70°C, a top pressure of 70 kPa, a bottom temperature of 80°C, a bottom pressure of 85 kPa, and a reflux ratio of 3.

[0097] S5. Pump 55% of the diluted liquor flow rate obtained from S2 into the second distillation column for second distillation (separation of ethanol and water). Collect the ordinary grade liquor product from the top of the second distillation column, collect the wastewater from the bottom of the column (the wastewater is returned to the slurry preparation system for recycling), and collect the material containing fusel oil from the side stream of the column into the fusel oil washing tank. The fusel oil is collected as a by-product and output.

[0098] The conditions for the second distillation include: a top temperature of 115°C, a top pressure of 200 kPa, a bottom temperature of 130°C, a bottom pressure of 300 kPa, and a reflux ratio of 5.

[0099] Example 4

[0100] The method is the same as in Example 1, except that the conditions for primary distillation in S1 are different. Specifically, the bottom temperature of the crude distillation column is adjusted to 95°C, and the top temperature of the crude distillation column is adjusted to 75°C.

[0101] Example 5

[0102] The method is the same as in Example 1, except that the washing conditions are different in S2. Specifically, in S2, the weight ratio of water to crude wine is 0.5:1, and the ethanol content in the diluted wine produced from the washing tower is 25 wt%.

[0103] Example 6

[0104] The method is the same as in Example 1, except that the conditions for the first distillation in S3 are different. Specifically, in S3, during the first distillation, the reflux ratio is 1, the top pressure is 380 kPa, the top temperature is 128°C, and the reflux ratio is 2.

[0105] Example 7

[0106] The method is the same as in Example 1, except that the conditions for the second distillation are different in S5. Specifically, in S5, when ethanol and water are separated in the second distillation column, the pressure at the top of the column is 120 kPa and the temperature at the top of the column is 93°C.

[0107] Comparative Example 1

[0108] This comparative example illustrates the method of producing premium / standard wine products using the traditional 6-tower process.

[0109] The traditional 6-tower process for producing premium / standard wine products is as follows: Figure 2As shown. The specific operating steps are as follows: After the raw material enters the crude distillation column, part of the gas at the top of the column enters the auxiliary crude distillation column to remove light impurities; the liquid phase at the top of the column is collected and enters the water washing column; the diluted liquor obtained after water washing enters the rectification column; the top of the rectification column is collected and enters the methanol column; the premium liquor product is obtained from the bottom of the methanol column; the side streams from the rectification column and the methanol column are collected and enter the recovery column; the industrial liquor is collected at the top of the recovery column; the ethanol at the bottom of the column can be returned to the water washing column for recovery.

[0110] The crude distillation column uses fresh steam, and the overhead gas from this column mainly serves as a heat source for the water washing column; the overhead gas from the water washing column serves as a heat source for the crude distillation column and the methanol column; the fresh steam also serves as a heat source for the auxiliary crude distillation column and the recovery column.

[0111] The specific operating parameters of each tower in Comparative Example 1 are shown in Table 1.

[0112] Table 1

[0113]

[0114]

[0115] Test Example 1

[0116] The quality of the premium and ordinary grade wine products prepared in each example and comparative example was measured, and the results are shown in Table 2.

[0117] The quality of ordinary grade wine products must meet the national standard for edible alcohol, GB / T 10343-2008.

[0118] The quality of premium-grade wine products must meet the national standard for edible alcohol, GB / T 10343-2008, which specifies the standards for premium-grade wine.

[0119] Test Example 2

[0120] Steam consumption, energy consumption, and ethanol yield were measured for each example and comparative example, and the results are shown in Table 3.

[0121] Steam consumption (t / t ethanol) = Steam required for the whole process (t) ÷ Total ethanol production of each product (t).

[0122] Ethanol yield (%) = Total ethanol content in each product ÷ Total ethanol content in fermented mash.

[0123] The formula for calculating energy consumption (MJ / t ethanol) is: calorific value of steam (MJ) × steam consumption.

[0124] Heat of vaporization of steam: The pressure of fresh steam at the distillation boundary is 8 kgG. The energy conversion value at this pressure is: the conversion value of 1 ton of steam is 76 kg of standard oil (the low calorific value of 1 kg of standard oil is 41.868 MJ, so the conversion value of 1 ton of steam is 3182 MJ. For details, see GB / T-50441).

[0125] Table 2

[0126]

[0127]

[0128] Table 2 (continued)

[0129]

[0130]

[0131] Table 3

[0132]

[0133] As can be seen from the results of Examples 1-3 in Tables 2-3, the premium and ordinary wines prepared by the method of the present invention meet the national standards. At the same time, it can further reduce energy consumption (reduce steam consumption and energy consumption) and increase ethanol yield. In the preferred embodiment, energy consumption is reduced by 20% and ethanol yield is as high as 99%.

[0134] Compared with the previous example, the temperature at the top and bottom of the crude distillation column in Example 4 was higher, which caused the acid and ester substances at the bottom of the crude distillation column to be distilled to the top of the column. As a result, the acid and ester content in the obtained premium wine and ordinary wine products exceeded the standard, the product quality did not meet the standard, and the energy consumption was high.

[0135] Compared with the previous example, the amount of water used for washing in Example 5 was less, resulting in poor washing effect and insufficient discharge of fusel alcohols at the top of the washing tower. Consequently, the content of isopropanol in the obtained premium and ordinary wine products exceeded the standard, and the product quality did not meet the standard.

[0136] Compared with the previous example, in Example 6, the top pressure, top temperature, and reflux ratio of the first distillation column were reduced, and the bottom heat supply of the second distillation column was insufficient (because the top vapor of the first distillation column is used as a heat source for the second distillation column, the distillation temperature and reflux ratio of the first distillation column decreased, and the temperature and reflux ratio of the second distillation column also had to be reduced), resulting in the content of substances such as isopropanol in the prepared ordinary grade wine exceeding the standard, and qualified products could not be produced.

[0137] Compared with the previous example, the pressure and temperature at the top of the second distillation column in Example 7 are reduced, which makes the vapor temperature at the top of the second distillation column lower than the temperature at the bottom of the water washing column (the temperature difference between the second distillation column and the water washing column is generally 10°C, and the minimum temperature difference should be higher than 5°C). As a result, the water washing column cannot be used as a heat source, and thus the premium and ordinary wine products cannot be obtained.

[0138] Compared with the examples, Comparative Example 1 uses a traditional 6-tower process to produce premium and regular wine products, which has high energy consumption and low ethanol yield.

[0139] In summary, the method of this invention can simultaneously produce high-quality ordinary and premium wine products, with low energy consumption and high ethanol yield.

[0140] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A method for the joint production of ordinary-grade and premium-grade wines, characterized in that, The method includes: S1. The fermented mash is subjected to primary distillation to obtain crude liquor; S2. Wash the crude wine obtained in S1 with water to obtain a light wine; S3. At least a portion of the light wine obtained in S2 is subjected to a first distillation to obtain a purified and concentrated liquid; S4. Remove methanol from the purified and concentrated liquid obtained in S3 to obtain a premium wine product. S5. At least a portion of the light liquor obtained in S2 is subjected to a second distillation to obtain a standard grade liquor product. The distillation temperature of the second distillation is 30-50°C higher than that of the primary distillation, and the distillation temperature of the first distillation is 30-45°C higher than that of the second distillation.

2. The method according to claim 1, wherein, In S1, the primary distillation method includes: performing primary distillation on the fermentation mash in a crude distillation column to obtain the overhead gas of the crude distillation column, the bottom material of the crude distillation column, and crude liquor; Preferably, the conditions for the primary distillation include: a top pressure of 25 kPa to 35 kPa and a top temperature of 45-70°C; a bottom pressure of 35 kPa to 60 kPa and a bottom temperature of 75-90°C; and a reflux ratio of 0.3-0.

7.

3. The method according to claim 1 or 2, wherein, In S2, when the water washing is performed, the amount of water used is such that the weight ratio of water to crude wine is (1-4):1, preferably (1-2.5):1; And / or, based on the total mass of the light wine, in S3, the flow rate of the light wine for the first distillation is 40-50 wt%; in S5, the flow rate of the light wine for the second distillation is 50-60 wt%.

4. The method according to any one of claims 1-3, wherein, In S2, the water washing method includes: washing the crude wine with water in a water washing tower to remove fusel oil and n-propanol from the crude wine, thereby obtaining a light wine; Preferably, the washing conditions include: a tower top pressure of 100 kPa to 120 kPa and a tower top temperature of 85-92°C; a tower bottom pressure of 110 kPa to 140 kPa and a tower bottom temperature of 90-100°C; and a reflux ratio of 1-3. Preferably, the ethanol content in the light wine is 10-20 wt%.

5. The method according to any one of claims 1-4, wherein, In S3, the first distillation method includes: in a first distillation column, purifying and concentrating at least a portion of the light wine obtained in S2 to obtain purified and concentrated liquid, fusel oil-containing material, and column bottom wastewater.

6. The method according to claim 5, wherein, The conditions for the first distillation include: a top pressure of 400 kPa to 450 kPa and a top temperature of 130-140°C; a bottom pressure of 420 kPa to 520 kPa and a bottom temperature of 150-160°C; and a reflux ratio of 3-8.

7. The method according to any one of claims 1-5, wherein, In S4, the method for removing methanol includes: removing methanol from the purified and concentrated liquid obtained in S3 in a methanol tower to obtain a premium wine product.

8. The method according to claim 7, wherein, The conditions for methanol removal include: a top pressure of 50 kPa to 70 kPa and a top temperature of 60-70°C; a bottom pressure of 75 kPa to 85 kPa and a bottom temperature of 68-80°C; and a reflux ratio of 1-3.

9. The method according to any one of claims 1-6, wherein, In S5, the second distillation method includes: in a second distillation column, separating at least a portion of the light wine obtained in S2 into ethanol and water to obtain a standard-grade wine product, fusel oil-containing material, and column bottom wastewater.

10. The method according to claim 9, wherein, The conditions for the second distillation include: a top pressure of 160 kPa to 200 kPa and a top temperature of 105-115°C; a bottom pressure of 200 kPa to 300 kPa and a bottom temperature of 120-130°C; and a reflux ratio of 2-5.

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