CN111925043B - Device and method for producing food drinking grade light water - Google Patents
Device and method for producing food drinking grade light water Download PDFInfo
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- CN111925043B CN111925043B CN202010928477.1A CN202010928477A CN111925043B CN 111925043 B CN111925043 B CN 111925043B CN 202010928477 A CN202010928477 A CN 202010928477A CN 111925043 B CN111925043 B CN 111925043B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 404
- 235000013305 food Nutrition 0.000 title claims abstract description 112
- 230000035622 drinking Effects 0.000 title claims abstract description 88
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 239000002994 raw material Substances 0.000 claims abstract description 122
- YZCKVEUIGOORGS-OUBTZVSYSA-N Deuterium Chemical compound [2H] YZCKVEUIGOORGS-OUBTZVSYSA-N 0.000 claims abstract description 101
- 229910052805 deuterium Inorganic materials 0.000 claims abstract description 101
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 50
- 239000011707 mineral Substances 0.000 claims abstract description 50
- 239000008235 industrial water Substances 0.000 claims abstract description 43
- 239000000047 product Substances 0.000 claims description 185
- 238000010992 reflux Methods 0.000 claims description 108
- 239000007788 liquid Substances 0.000 claims description 107
- 239000007789 gas Substances 0.000 claims description 68
- 239000000498 cooling water Substances 0.000 claims description 28
- 238000009833 condensation Methods 0.000 claims description 22
- 230000005494 condensation Effects 0.000 claims description 22
- 238000013016 damping Methods 0.000 claims description 20
- 238000002156 mixing Methods 0.000 claims description 16
- 239000000203 mixture Substances 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 13
- 238000004659 sterilization and disinfection Methods 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 12
- 235000013361 beverage Nutrition 0.000 claims description 11
- 239000006227 byproduct Substances 0.000 claims description 10
- 239000002440 industrial waste Substances 0.000 claims description 10
- 230000001954 sterilising effect Effects 0.000 claims description 10
- 238000004891 communication Methods 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 9
- 239000008399 tap water Substances 0.000 claims description 9
- 235000020679 tap water Nutrition 0.000 claims description 9
- 230000008020 evaporation Effects 0.000 claims description 7
- 238000009825 accumulation Methods 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims description 5
- 230000009286 beneficial effect Effects 0.000 claims description 4
- 238000012856 packing Methods 0.000 claims description 4
- 239000012535 impurity Substances 0.000 claims description 3
- 101150049281 PRM1 gene Proteins 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000007599 discharging Methods 0.000 claims 4
- 235000020188 drinking water Nutrition 0.000 claims 1
- 239000003651 drinking water Substances 0.000 claims 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 abstract description 5
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 5
- 229910001424 calcium ion Inorganic materials 0.000 abstract description 5
- 239000011777 magnesium Substances 0.000 abstract description 5
- 229910001425 magnesium ion Inorganic materials 0.000 abstract description 5
- 235000020510 functional beverage Nutrition 0.000 abstract description 4
- 238000005516 engineering process Methods 0.000 description 5
- 239000012263 liquid product Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N Heavy water Chemical compound [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- 238000003491 array Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000009982 effect on human Effects 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/043—Details
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/046—Treatment of water, waste water, or sewage by heating by distillation or evaporation under vacuum produced by a barometric column
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/68—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water
- C02F1/683—Treatment of water, waste water, or sewage by addition of specified substances, e.g. trace elements, for ameliorating potable water by addition of complex-forming compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
Abstract
The device for producing the light water of the food drinking level at least comprises a stripping cascade tower system, an enrichment cascade tower system, a storage system of the light water of the food drinking level and a system vacuumizing system, wherein the stripping cascade tower system consists of a stripping cascade tower-I-a stripping cascade tower-n which are serially connected in front and back, and the bottom of the stripping cascade tower system is provided with heat source water of a reboiler for removing a large amount of deuterium water (D 2 O), the obtained product is used as a raw material source for enriching the drinking grade light water of food. The invention purifies industrial water and reduces hardness (removes magnesium and calcium ions) to be used as a primary production raw material of the food drinking grade light water, and realizes the industrial scale production of the food drinking grade light water by cascade vacuum rectification. The device adopts the cascade towers, and realizes the production of the light water with different abundance foods and drinking grades by arranging the regular towers and the bulk towers with different grades in series/parallel connection. The light water of the product can be used as food drinking grade light water by adding minerals, and can be directly drunk or used as raw material water of other functional beverages.
Description
Technical Field
The invention relates to a device and a method for producing food drinking grade light water, belonging to the field of light water production.
Background
With the development of society, the importance of the national health is increasing. Deuterium depleted is an important feature of food and beverage grade light water as opposed to any other common body of water. Deuterium isotopes, which contain hydrogen in all natural bodies of water on earth, are harmful to organisms regardless of the deuterium content. As long as a part of deuterium is slightly removed from normal water, the effect on human health cannot be estimated, so that more and more people choose to drink food and drink grade light water as daily health care. The invention reduces the deuterium content (D/(D+H) in water by vacuum rectification means not more than 20-30 ppm) and produces the food drinking grade light water beneficial to human health.
Disclosure of Invention
The invention relates to a technology and a device for producing food drinking grade light water, which are used for purifying and hardness-reducing (magnesium and calcium ion removal) industrial water as a production raw material of the food drinking grade light water and realize the industrial scale production of the food drinking grade light water by cascade vacuum rectification. The device adopts the cascade towers, and realizes the production of the light water with different abundance foods and drinking grades by arranging the regular towers and the bulk towers with different grades in series/parallel connection. The light water of the product can be used as food drinking grade light water by adding minerals, and can be directly drunk or used as raw material water of other functional beverages. The purpose of the invention is obtained by the following technical scheme: food drinking grade light aquatic product The device for producing the deuterium oxide comprises at least four parts of a stripping cascade tower system, an enrichment cascade tower system, a food drinking grade light water storage system and a system vacuumizing system, wherein the stripping cascade tower system comprises a stripping cascade tower-I-a stripping cascade tower-n which are serially connected in front and back, and the bottom of the stripping cascade tower system is provided with reboiler heat source water for removing a large amount of deuterium water (D 2 O), the obtained product is used as a raw material source for enriching the food drinking grade light water, the enriching cascade tower system consists of an enriching cascade tower-I-enriching cascade tower-X, the top of the enriching cascade tower system is provided with condenser cold source water, the low-abundance food drinking grade light water at the top of the stripping cascade tower is used as a raw material, and a random packing tower is used as a rectifying tower to produce the high-abundance sequence food drinking grade light water. The food drinking grade light water storage system completes the subsequent treatment of the product light water, including adding minerals beneficial to human body and UV disinfection of water body.
As preferable: the raw material required by the storage system is a raw material water tank, the outlet of the raw material water tank is connected with the inlet of a raw material outlet stop valve, the outlet of the raw material outlet stop valve is connected with the inlet of a raw material water softening tank, the outlet of the raw material water softening tank is connected with the inlet of a raw material buffer tank, the raw material buffer tank is connected with the raw material inlet of a stripping cascade tower-I through the stop valve, and the top exhaust port of the stripping cascade tower-I is connected with the exhaust gas exhaust buffer tank inlet through an exhaust gas exhaust stop valve; the outlet of the exhaust gas emission buffer tank is connected with the hot end inlet of the stripping cascade tower-I condenser, the outlet of the hot end of the condenser is connected with the inlet of the condensed reflux buffer tank through a converging stop valve, the outlet of the condensed reflux buffer tank is connected with a reflux damping inlet, the reflux damping outlet is connected with the reflux inlet of the stripping cascade tower-I, the cold end inlet of the condenser is connected with the cold end outlet of the condenser, the cold end outlet of the condenser is connected with the cooling water inlet of the raw material water tank through a cooling water inlet stop valve, the cold end inlet of the condenser is connected with an industrial tap water pipe network, and the hot end inlet of the condenser is respectively connected with the hot end outlet of the condenser and the inlet of the converging stop valve; the hot end outlet of the condenser is connected with the inlet of the food drinking grade light water storage sequence.
As preferable: the liquid level communication stop valve at the bottom of the stripping cascade tower-I is connected with the overflow port of the stripping cascade tower-I, the liquid level communication stop valve at the bottom of the stripping cascade tower-I and the liquid outlet stop valve at the bottom of the stripping cascade tower-I are respectively connected with the cold end inlet of the reboiler, the cold end outlet of the reboiler is connected with the reboiling gas inlet at the bottom of the stripping cascade tower-I, the hot end inlet of the reboiler is connected with the cold end outlet of the heat exchanger, and the cold end inlet of the heat exchanger is connected with cooling water. The hot end inlet of the heat exchanger is connected with an industrial waste heat source, the hot end outlet of the heat exchanger is connected with an industrial waste discharge port, the inlet of the stop valve and the inlet of the stop valve are jointly connected with a liquid outlet at the bottom of the stripping cascade tower-I, the outlet of the stop valve is connected with an inlet of a class I heavy deuterium water collecting tank, a flowmeter is arranged at the inlet of the class I heavy deuterium water collecting tank, and the raw material inlet (Pdn-1) of the stripping cascade tower-n is connected with a food drinking grade light water storage sequence outlet. The top exhaust port of the stripping cascade tower-n is connected with the inlet of the exhaust gas emission buffer tank through an exhaust gas emission stop valve; the outlet of the exhaust gas discharge buffer tank is connected with the hot end inlet of the stripping cascade tower-n condenser, and the hot end outlet of the condenser is connected with the inlet of the condensed reflux buffer tank through a converging stop valve. The outlet of the condensed reflux buffer tank is connected with a reflux damping inlet, and the reflux damping outlet is connected with a reflux liquid inlet of the stripping cascade tower-n. The cold end inlet of the condenser is connected with the cold end outlet of the condenser, and the cold end outlet of the condenser is connected with the cooling water inlet of the raw material water tank through the cooling water inlet stop valve. The cold end inlet of the condenser is connected with an industrial tap water pipe network. The hot end inlet of the condenser is respectively connected with the hot end outlet of the condenser and the inlet of the confluence stop valve; the hot end outlet of the condenser is connected with the inlet of the food drinking grade light water storage sequence.
As preferable: the liquid level communication stop valve at the bottom of the stripping cascade tower-n is connected with the overflow port of the stripping cascade tower-n, the liquid level communication stop valve at the bottom of the stripping cascade tower-n and the liquid outlet stop valve at the bottom of the stripping cascade tower-n are respectively connected with the cold end inlet of the reboiler, and the cold end outlet of the reboiler is connected with the reboiling gas inlet at the bottom of the stripping cascade tower-n. The hot end inlet of the reboiler is connected with the cold end outlet of the heat exchanger. The inlet of the stop valve and the inlet of the stop valve are jointly connected with a liquid outlet at the bottom of the stripping cascade tower-n, the outlet of the stop valve is connected with an inlet of an n-class heavy deuterium water collecting tank, a flowmeter is arranged at the inlet of the n-class heavy deuterium water collecting tank, and the raw material inlet (Pdn) of the enrichment cascade tower-I is connected with a raw material inlet of a food and drink grade light water storage sequence. The top exhaust port of the enrichment cascade tower-I is connected with the inlet of the exhaust gas emission buffer tank through an exhaust gas emission stop valve; the outlet of the exhaust gas discharge buffer tank is connected with the hot end inlet of the condenser of the enrichment cascade tower-I, and the hot end outlet of the condenser is connected with the inlet of the condensed reflux buffer tank through a converging stop valve. The outlet of the condensed reflux buffer tank is connected with a reflux damping inlet, and the reflux damping outlet is connected with a reflux liquid inlet of the enrichment cascade tower-I. The cold end inlet of the condenser is connected with the cold end outlet of the condenser, and the cold end outlet of the condenser is connected with the cooling water inlet of the raw material water tank through the cooling water inlet stop valve. The cold end inlet of the condenser is connected with an industrial tap water pipe network. The hot end inlet of the condenser is respectively connected with the hot end outlet of the condenser and the inlet of the confluence stop valve; the hot end outlet of the condenser is connected with the inlet of the food drinking grade light water storage sequence.
As preferable: the bottom liquid outlet of the enrichment cascade tower-I is connected with the inlet of a stop valve, the outlet of the stop valve is connected with the inlet of a class I light deuterium water collecting tank, a flowmeter is arranged at the inlet of class m light deuterium water, the raw material inlet (Prm-1) of the enrichment cascade tower-m is connected with the raw material outlet of a food drinking grade light water storage sequence, and the exhaust outlet at the top of the enrichment cascade tower-m is connected with the inlet of an exhaust gas exhaust buffer tank through an exhaust gas exhaust stop valve; the outlet of the exhaust gas emission buffer tank is connected with the hot end inlet of the enrichment cascade tower-m condenser, the hot end outlet of the condenser is connected with the inlet of the condensation reflux buffer tank through a converging stop valve, the outlet of the condensation reflux buffer tank is connected with the reflux damping inlet, the reflux damping outlet is connected with the reflux inlet of the enrichment cascade tower-m, the cold end inlet of the condenser is connected with the cold end outlet of the condenser, the cold end outlet of the condenser is connected with the cooling water inlet of the raw material water tank through a cooling water inlet stop valve, the cold end inlet of the condenser is connected with an industrial tap water pipe network, and the hot end inlet of the condenser is respectively connected with the hot end outlet of the condenser and the converging stop valve inlet; the hot end outlet of the condenser is connected with the inlet of the food drinking grade light water storage sequence,
and the liquid outlet at the bottom of the enrichment cascade tower-m is connected with the inlet of a stop valve, the outlet of the stop valve is connected with the inlet of an m-class light deuterium water collecting tank, and a flowmeter is arranged at the inlet of the m-class light deuterium water collecting tank. The reboiler and the hot end outlet of the reboiler are connected with the inlet of a raw material pump, and the raw material pump is connected with the inlet of a raw material water tank through a stop valve.
As preferable: the enrichment cascade column-x feed inlet (Prx-1) is connected to the food and beverage grade light water storage sequence feed outlet. The top exhaust port of the enrichment cascade tower-x is connected with the hot end inlet of the enrichment cascade tower-x condenser through an exhaust gas discharge stop valve, and the hot end outlet of the condenser is respectively connected with the reflux liquid inlet of the enrichment cascade tower-x and the stop valve inlet. The outlet of the stop valve is connected with the inlet of the food drinking grade light water storage sequence. The cold end inlet of the condenser is connected with an industrial tap water pipe network, and the cold end outlet of the condenser is connected with the cooling water inlet of the raw material water tank through a cooling water inlet stop valve. The liquid outlet at the bottom of the enrichment cascade tower-x is connected with the inlet of the stop valve, the outlet of the stop valve is connected with the inlet of the food and drink grade light water storage sequence, and a flowmeter is arranged on the flow path.
As preferable: the collecting tank of the stripping cascade tower-I, the collecting tank of the stripping cascade tower-n and the collecting tank of the enrichment cascade tower-I are respectively connected with the inlet of the heavy deuterium water storage tank, the heavy deuterium water storage tank) is discharged through the stop valve, and the system vacuumizing port is respectively arranged at the top of the exhaust gas discharge buffer tank, the top of the exhaust gas discharge buffer tank and the outlet of the exhaust gas discharge stop valve.
The method of the device for producing the food drinking grade light water comprises the following steps:
step 1: the rectification operation pressure in all the device towers is controlled to be 200-250 mmHg, a rotary vane vacuum pump is needed to be used for vacuumizing the whole device before the device is started, the system vacuumizing ports V1-V5 are arranged at the top exhaust discharge stop valves of the stripping cascade tower-I-stripping cascade tower-n and the enrichment cascade tower-I-enrichment cascade tower-x, the exhaust discharge stop valve, the raw material outlet stop valve, the cooling water inlet stop valve and the stop valve are opened, the stop valve and the stop valve are opened, and the vacuumizing is ended when the pressure near the vacuum pump pumping port is reduced below 5KPa, and the valves are closed again. Ensuring that all valves are in a closed state.
Step 2: and opening a raw material outlet stop valve, and allowing raw material water to enter a raw material buffer tank after the hardness of the raw material water is reduced and impurities are removed through a raw material water softening tank. And opening a stop valve, enabling raw material water to enter a stripping cascade tower-I, opening the stop valve, and evaporating liquid accumulation at the bottom of the stripping cascade tower-I. Then the exhaust gas discharge shutoff valve is opened, and the evaporated gas is partially condensed in the condenser. The gas-liquid mixture has two paths: (1) and opening a confluence stop valve, and enabling condensate to enter a condensed reflux buffer tank to serve as reflux. In order to make the reflux liquid of each parallel tube column in the stripping cascade tower-I consistent, a reflux damping is arranged at a reflux liquid port; (2) the vapor which is not condensed water enters a condenser, and enters a food drinking grade light water storage sequence as a product sequence after condensation. The cold source of the condenser is normal-temperature industrial water, a cooling water inlet stop valve is opened, and the normal-temperature industrial water enters the raw material water tank. The heavy deuterium water at the bottom of the rectifying byproduct stripping cascade tower-I is introduced into a class I heavy deuterium water collection tank by opening a stop valve, and then is collected into a heavy deuterium water storage tank. The heavy deuterium water flow at the bottom of the stripping cascade tower-I is measured by a flowmeter, and in order to maintain the stable liquid level of the accumulated liquid at the bottom of the stripping cascade tower-I, a liquid level communicating stop valve at the bottom of the stripping cascade tower-I is opened, so that water overflowing a specified liquid level can be introduced into a reboiler.
Step 3: each stage of stripping cascade operates similarly to stripping cascade-I. Starting from the stripping cascade-II, the feed water of each stage originates from the product at the top of the preceding stage. The raw water of the stripping cascade tower-n is derived from the product at the top of the stripping cascade tower-n-1. And opening a stop valve, and evaporating the liquid product at the bottom of the stripping cascade tower-n. Then the exhaust gas discharge shutoff valve is opened, and the evaporated gas is partially condensed in the condenser. The gas-liquid mixture has two paths: (1) and opening a confluence stop valve, and enabling condensate to enter a condensed reflux buffer tank to serve as reflux. In order to make the reflux liquid of each parallel tube column in the stripping cascade tower-n consistent, a reflux damping is arranged at a reflux liquid port; (2) the vapor which is not condensed water enters a condenser, and enters a food drinking grade light water storage sequence as a product sequence after condensation. The cold source of the condenser is normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank after exiting the condenser.
Step 4: the heavy deuterium water at the bottom of the rectification byproduct stripping cascade tower-n is introduced into n types of heavy deuterium water collection tanks by opening a stop valve, and then is collected into the heavy deuterium water storage tanks. The flow rate of heavy deuterium water at the bottom of the stripping cascade tower-n is measured by a flowmeter, and similar to other stripping cascade towers, in order to maintain the stable liquid level of accumulated liquid at the bottom of the stripping cascade tower-n, a liquid level communication stop valve at the bottom of the stripping cascade tower-n is opened, so that water overflowing a specified liquid level can be introduced into a reboiler, and the heat source of the reboiler at the bottom of the stripping cascade tower is derived from industrial waste heat. The industrial water and the boiled water exchange heat in the heat exchanger, so that the boiled water absorbs the industrial waste heat and is used as a heat source of the reboiler. The stop valve is opened, and the boiled water discharged from the reboiler is introduced into the raw material water tank by the water pump.
Step 5: the top product of the stripping cascade tower-n is used as the raw material of the enrichment cascade tower-I. The electric heater of the enrichment cascade tower-I is electrified to work, and the bottom effusion is evaporated. The exhaust gas discharge shutoff valve is opened, and the overhead evaporation gas is partially condensed in the condenser. The gas-liquid mixture has two paths: (1) and opening a confluence stop valve, and enabling condensate to enter a condensed reflux buffer tank to serve as reflux. In order to make the reflux liquid of each parallel tube column in the enrichment cascade column-I consistent, a reflux liquid port is provided with reflux damping; (2) the vapor which is not condensed water enters a condenser, and enters a food drinking grade light water storage sequence as a product sequence after condensation. The cold source of the condenser is normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank after exiting the condenser.
Step 6: the heavy deuterium water at the bottom of the rectification byproduct enrichment cascade tower-I is introduced into an r-type heavy deuterium water collection tank by opening a stop valve, and then is collected into a heavy deuterium water storage tank. The flow rate of heavy deuterium water at the bottom of the enrichment cascade tower-I is measured by a flowmeter, and the operation process of each enrichment cascade tower is similar to that of the enrichment cascade tower-I. Starting from the enrichment cascade column-II, the feed water of each stage originates from the product at the top of the preceding stage. The raw water of the enrichment cascading tower-m is derived from the product at the top of the enrichment cascading tower-m-1. The electric heater of the enrichment cascade tower-m is electrified to work, and the bottom effusion is evaporated. The exhaust gas discharge shutoff valve is opened, and the overhead evaporation gas is partially condensed in the condenser. The gas-liquid mixture has two paths: (1) and opening a confluence stop valve, and enabling condensate to enter a condensed reflux buffer tank to serve as reflux. In order to make the reflux liquid of each parallel tubular tower in the enrichment cascade tower-m consistent, a reflux damping is arranged at a reflux liquid port; (2) the vapor which is not condensed water enters a condenser, and enters a food drinking grade light water storage sequence as a product sequence after condensation. The cold source of the condenser is normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank after exiting the condenser.
Step 7: starting from the post-rectifying column of the enrichment cascade column-I, the bottom liquid product is not collected to the heavy deuterium water storage tank any more, but is used as a product sequence of the food and drink grade light water. The light deuterium water at the bottom of the rectification byproduct enrichment cascade tower-m is introduced into a Pbrm light deuterium water collection tank by opening a stop valve, and then enters a food and drink grade light water storage sequence. The light deuterium water flow at the bottom of the enrichment cascade tower-m is measured by a flowmeter, and the raw water of the final enrichment cascade tower-x is derived from the tower top product of the enrichment cascade tower-x-1. The raw water of the final enrichment cascading tower-x is derived from the product at the top of the enrichment cascading tower-x-1. The electric heater of the final enrichment cascade tower-x is electrified to work, and the bottom effusion is evaporated. The exhaust gas discharge shutoff valve is opened, and the overhead evaporation gas is totally condensed in the condenser. The condensed liquid has two paths: (1) opening a stop valve, and enabling condensate to enter a food drinking grade light water storage sequence; (2) the rest condensate is returned to the final enrichment cascade column-x as reflux liquid. The cold source of the condenser is normal temperature industrial water, the normal temperature industrial water enters the raw material water tank after exiting the condenser, and the products collected from the device are finally collected into a food drinking grade light water storage sequence. From stripping cascade-I to stripping cascade-n, there is a special product collection tank; from the enrichment cascade column-I to the enrichment cascade column-x, the enrichment cascade column has two product collection tanks except for the enrichment cascade column-I.
Step 8: the method comprises the steps of opening a stop valve, collecting the top product of the stripping cascade tower-I into a product collecting tank, opening the stop valve, collecting the top product of the stripping cascade tower-n into the product collecting tank, opening the stop valve, collecting the top product of the enrichment cascade tower-I into the product collecting tank, opening the stop valve, collecting the top product of the enrichment cascade tower-m into the product collecting tank, and opening the stop valve. Opening a stop valve, and collecting light deuterium water at the bottom of the enrichment cascade tower-m into a product collecting tank; the stop valve is opened, light deuterium water at the bottom of the enrichment cascade tower-x is collected into a product collecting tank, and liquid discharged from the product collecting tank at the top of the enrichment cascade tower-i-x is divided into two paths: (1) and opening a stop valve, starting a water pump, and removing the top product of the stripping cascade tower-I to the next stage of rectifying tower to serve as a raw material. And opening a stop valve, starting a water pump, and removing the product at the top of the stripping cascade tower-n to the next stage of rectifying tower to serve as a raw material. And opening a stop valve, starting a water pump, and enriching the tower top product of the cascade tower-I to go to the next stage of rectifying tower to be used as a raw material. And opening a stop valve, starting a water pump, and enriching the product at the top of the cascade tower-m to the next stage of rectifying tower to be used as a raw material. Opening a stop valve, starting a water pump, and enriching the product at the top of the cascade tower-x to go to the next stage of rectifying tower to be used as a raw material; (2) opening a stop valve), feeding the product at the top of the stripping cascade tower-I into a water tank, opening the stop valve, mixing the product at the top of the stripping cascade tower-I with high-concentration mineral solution, adding minerals into the product, and feeding the product into a water body purifying tank; opening a stop valve, feeding the product at the top of the stripping cascade tower-n into a water tank, opening the stop valve, mixing the product at the top of the stripping cascade tower-n with high-concentration mineral solution, adding minerals into the product, and feeding the product into a water body purifying tank; opening a stop valve, enabling the tower top product of the enrichment cascade tower-I to enter a water tank, opening the stop valve, mixing the tower top product of the enrichment cascade tower-I with a high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank; opening a stop valve, enabling the product at the top of the enrichment cascade tower-m to enter a water tank, opening the stop valve, mixing the product at the top of the enrichment cascade tower-m with high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank; opening a stop valve, enabling the product at the top of the enrichment cascade tower-x to enter a water tank, opening the stop valve, mixing the product at the top of the enrichment cascade tower-x with high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank; the method comprises the steps of opening a stop valve, enabling light deuterium water at the bottom of an enrichment cascade tower-m to enter a water tank, opening the stop valve, enabling light deuterium water at the bottom of the enrichment cascade tower-m to be mixed with high-concentration mineral solution, adding minerals into a product, and entering a water purification tank, opening the stop valve, enabling light deuterium water at the bottom of the enrichment cascade tower-x to enter the water tank, opening the stop valve, enabling light deuterium water at the bottom of the enrichment cascade tower-x to be mixed with high-concentration mineral solution, adding minerals into the product, entering the water purification tank, enabling UV sterilization of products at the bottom of the stripping cascade tower-I-stripping cascade tower-n in the water purification tank, opening the stop valve (for outputting food drinking grade light water, enabling UV sterilization of products at the bottom of the enrichment cascade tower-I-enrichment cascade tower-x in the water purification tank, opening the stop valve, outputting food drinking grade light water, enabling UV sterilization of products at the bottom of the rest of the enrichment cascade tower in the water purification tank, and opening the stop valve, and outputting the food drinking grade light water.
The utility model relates to a technology and a device for producing food drinking grade light water, which are used for purifying industrial water and reducing hardness (removing magnesium and calcium ions) to be used as a primary production raw material of the food drinking grade light water, and realize the industrial scale production of the food drinking grade light water by cascade vacuum rectification. The device adopts the cascade towers, and realizes the production of the light water with different abundance foods and drinking grades by arranging the regular towers and the bulk towers with different grades in series/parallel connection. The light water of the product can be used as food drinking grade light water by adding minerals, and can be directly drunk or used as raw material water of other functional beverages.
Drawings
FIG. 1 is a schematic diagram of the construction of the present utility model.
Fig. 2 is a schematic diagram of food drinking grade light water storage.
Detailed Description
The utility model will be described in detail with reference to the accompanying drawings, as shown in fig. 1, the technology and the device for producing the food drinking grade light water at least comprise four parts, namely a stripping cascade tower system, an enrichment cascade tower system, a food drinking grade light water storage system and a system vacuumizing system. Wherein the stripping cascade tower system consists of high-efficiency structured packing towers which are serially connected in front and back and are used for removing a large amount of deuterium water (D 2 O), the obtained product is used as a raw material source for enriching the drinking grade light water of food. The enrichment cascade tower system takes low-abundance food drinking grade light water at the top of the stripping cascade tower as a raw material, and adopts a random packing tower as a rectifying tower to produce high-abundance sequence food drinking grade light water. The food drinking grade light water storage system completes the subsequent treatment of the product light water, including adding minerals beneficial to human body and UV disinfection of water body.
The raw water of the device has three sources: (1) industrial water; (2) heat source water of reboiler at the bottom of stripping cascade tower-I-stripping cascade tower-n; (3) stripping cascade tower-I-stripping cascade tower-n, enriching cascade tower-I-stripping cascade tower-x top condenser cold source water.
The stripping cascade towers-I to-n are connected in series, and each stage of stripping cascade tower is formed by connecting multiple tubes in parallel. According to the design of the technological process, the number of the tube arrays of each stage of stripping cascade tower is determined, and the optimal ratio of the number of the tube arrays between the front stage and the back stage is ensured (the highest separation efficiency in the rectification process is ensured, namely the maximum theoretical plate number is ensured.)
Further, heavy deuterium water accumulated at the bottoms of the stripping cascade towers-I to-n is collected and discharged out of the system. The reboiler heat sources at the bottoms of the stripping cascade towers-I to-n are industrial exhaust waste heat, and reboiling heat sources (industrial water) are heated by the industrial exhaust waste heat so as to realize reboiling of bottom liquid. The reboiling heat source (industrial water) can be used as the raw material water source of the device.
Further, the top exhaust condensation of the stripping cascade towers-I to-n is realized by normal-temperature industrial water. The top exhaust condensation of the stripping cascade towers-I to-n is divided into two processes: the first condenser is used for condensing the reflux liquid, and the second condenser is used for collecting light water in the factory product sequence. The product sequence light water condensed by the second condenser enters a food drinking grade light water storage sequence. And the liquid at the bottoms of the stripping cascade towers-I to-n are collected into a heavy deuterium water collecting tank.
The enrichment cascade towers-I to-x are connected in series, and each enrichment cascade tower is formed by connecting multiple columns of tubes in parallel. According to the design of the technological process, the number of the tubes of each stage of enrichment cascade tower is determined, and the optimal ratio of the number of the tubes between the front stage and the back stage is ensured (the highest separation efficiency in the rectification process is ensured, namely the maximum theoretical plate number is ensured.)
Further, the top exhaust condensation of the enrichment cascade tower-I-enrichment cascade tower-x is realized by normal-temperature industrial water. The top exhaust condensation of the enrichment cascade tower-I to the enrichment cascade tower-n is divided into two processes: the first condenser is used for condensing reflux liquid, and the second condenser is used for collecting light water in the product sequence. The product sequence light water condensed by the second condenser enters a food drinking grade light water storage sequence. Notably, the bottoms liquid of the enrichment cascading tower-m-enrichment cascading tower-x enters the food drinking grade light water storage sequence as the sequence light water.
As shown in fig. 2, the food drinking grade light water storage schematic diagram, the top products of the stripping cascade towers-I-stripping cascade tower-n, the top products of the enrichment cascade towers-I-enrichment cascade tower-x and the bottom light deuterium water of the enrichment cascade towers-m-enrichment cascade tower-x are stored in respective product collecting tanks, and part of the product collecting tanks are used as raw material sources of the next-stage rectifying tower; and mixing the rest part with the mineral concentrated solution, and performing UV sterilization to obtain qualified food drinking grade light water product.
Embodiments of the invention are as follows
The invention relates to a technology and a device for producing food drinking grade light water, which are used for purifying and reducing hardness (removing magnesium and calcium ions) of industrial water as a production raw material of the food drinking grade light water and realize the industrial scale production of the food drinking grade light water by cascade vacuum rectification. Before the device is started, all valves are closed.
The rectification operation pressure in the device tower is controlled to be 200-250 mmHg, the whole device needs to be vacuumized by using a rotary vane vacuum pump 77 before the device is started, and the system vacuumizing ports V1-V5 are arranged behind the exhaust gas discharge stop valves 16, 31, 44, 56 and 75 at the tops of the stripping cascade tower-I-stripping cascade tower-n and the enrichment cascade tower-I-enrichment cascade tower-x.
Further, the exhaust gas discharge shutoff valves 16, 31, 44, 56, 75, the raw material outlet shutoff valve 5, the cooling water inlet shutoff valve 4, and the shutoff valves 8, 13, 27, 40, 53, 64 are opened. The shut-off valves 77-82, 121, shut-off valves 90-94, shut-off valves 100-105, 122, and shut-off valves 109-111 in the food and beverage grade light water storage sequence 72 are opened. And when the pressure near the vacuum pump is reduced to below 5KPa, the vacuumizing is finished, and the valve is closed again.
The raw material outlet shutoff valve 5 is opened, and the raw material water passes through the raw material water softening tank 6 to reduce hardness and remove impurities, and then enters the raw material buffer tank 7. And opening a stop valve 8, and feeding raw water into the stripping cascade tower-I1.
Further, the stop valve 10 is opened, and the liquid product at the bottom of the stripping cascade column-I is evaporated. The exhaust gas discharge shutoff valve 16 is then opened, and the boil-off gas is partially condensed in the condenser 20. The gas-liquid mixture has two paths: (1) the confluence shut-off valve 21 is opened, and the condensate is introduced into the condensate reflux buffer tank 22 as reflux. In order to make the reflux liquid of each parallel tube column in the stripping cascade tower-I consistent, a reflux damping 17 is arranged at a reflux liquid port; (2) the non-condensed water vapor enters the condenser 23 and after condensation enters the food and beverage grade light water storage train 72 as a product train. The cold source of the condensers 20 and 23 is normal-temperature industrial water, the cooling water inlet stop valve 4 is opened, and the normal-temperature industrial water enters the raw material water tank 3.
Further, the heavy deuterium water at the bottom of the distillation byproduct stripping cascade-I1 is introduced into the class I heavy deuterium water collection tank 15 by opening the shut-off valve 13, and then collected into the heavy deuterium water storage tank 68. The flow of heavy deuterium water at the bottom of the stripping cascade-I1 is measured by a flow meter 14.
It is noted that, in order to maintain the liquid level of the liquid accumulation at the bottom of the stripping cascade-I1 stable, the water overflowing the prescribed liquid level can be introduced into the reboiler 9 by opening the liquid level communication stop valve 2 at the bottom of the stripping cascade-I1.
Each stage of stripping cascade operates similarly to stripping cascade-I1. Starting from the stripping cascade-II, the feed water of each stage originates from the product at the top of the preceding stage. The raw water of the stripping cascade tower-n 24 is derived from the product at the top of the stripping cascade tower-n-1. The shut-off valve 73 was opened and the bottom liquid product of the stripping cascade-n 24 was evaporated. Then, the exhaust gas discharge shutoff valve 31 is opened, and the evaporated gas is partially condensed in the condenser 33. The gas-liquid mixture has two paths: (1) the confluence shut-off valve 35 is opened and the condensate is introduced into the condensate reflux buffer tank 33 as reflux. In order to make the reflux liquid of each parallel tube column in the stripping cascade tower-n consistent, a reflux damping 30 is arranged at a reflux liquid port; (2) the non-condensed water vapor enters the condenser 36 and is condensed and enters the food and beverage grade light water storage train 72 as a product train. The cold sources of the condensers 30 and 33 are normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank 3 after exiting the condensers.
Further, the bottom heavy deuterium water of the distillation byproduct stripping cascade-n 24 is introduced into n kinds of heavy deuterium water collection tanks 29 by opening a shut-off valve 27, and then collected into a heavy deuterium water storage tank 68. The flow of heavy deuterium water at the bottom of the stripping cascade-n 24 is measured by a flow meter 27.
Similar to other stripping towers, in order to maintain stable liquid level in the bottom of stripping tower-n 24, the water overflowing the specified liquid level may be introduced into reboiler 26 by opening stop valve 25 communicating with the liquid level in the bottom of stripping tower-n 24.
It should be noted that the heat source of the reboiler at the bottom of the stripping cascade is derived from industrial waste heat. The industrial water exchanges heat with the boiled water in the heat exchanger 12, so that the boiled water absorbs industrial waste heat and is used as a heat source of a reboiler. The stop valve 108 is opened and the boiled water leaving the reboiler is introduced into the raw water tank 3 by the water pump 11.
The top product of the stripping cascade tower-n 24 is used as the raw material of the enrichment cascade tower-I37. The electric heater 38 of the enrichment cascade tower-I is powered on to evaporate the bottom liquid. The off-gas discharge shutoff valve 44 is opened and the overhead boil-off gas is partially condensed in the condenser 46. The gas-liquid mixture has two paths: (1) the confluence shut-off valve 48 is opened, and the condensate is introduced into the condensate reflux buffer tank 47 as reflux. In order to make the reflux liquid of each parallel tubular tower in the enrichment cascade tower-I37 consistent, a reflux damping 43 is arranged at a reflux liquid port; (2) the non-condensed water vapor enters the condenser 49 and is condensed and enters the food and beverage grade light water storage train 72 as a product train. The cold sources of the condensers 46 and 49 are normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank 3 after exiting the condensers.
Further, the heavy deuterium depleted water at the bottom of the rectifying by-product enrichment cascade-I37 is introduced into the r-type heavy deuterium depleted water collection tank 42 by opening the shut-off valve 40, and then collected into the heavy deuterium depleted water storage tank 68. The flow of heavy deuterium water at the bottom of the enrichment cascade column-I37 is metered by a flow meter 41.
Each stage of the enrichment cascade operates similarly to enrichment cascade-I37. Starting from the enrichment cascade column-II, the feed water of each stage originates from the product at the top of the preceding stage. The raw water of the enrichment cascading tower-m 50 is derived from the product at the top of the enrichment cascading tower-m-1. The enrichment cascade-m electric heater 52 is energized to evaporate the bottom liquid product. The off-gas discharge shutoff valve 56 is opened and the overhead boil-off gas is partially condensed in the condenser 58. The gas-liquid mixture has two paths: (1) the confluence shut-off valve 59 is opened and the condensate is fed to the condensate reflux buffer tank 60 as reflux. In order to make the reflux liquid of each parallel-connected tubular tower in the enrichment cascade tower-m 50 consistent, a reflux damping 55 is arranged at a reflux liquid port; (2) the non-condensed water vapor enters the condenser 61 and after condensation enters the food and beverage grade light water storage train 72 as a product train. The cold source of the condensers 58 and 61 is normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank 3 after exiting the condensers.
Further, it should be noted that starting from the post-rectifying column of the enrichment cascade column-I, the bottom product is no longer collected in the heavy deuterium depleted water storage tank 68, but rather is used as a product train for food and beverage grade light water. The light deuterium water at the bottom of the rectification by-product enrichment cascade-m 50 is introduced into a Pbrm type light deuterium water collection tank 67 by opening a shut-off valve 53, and then into a food and beverage grade light water storage sequence 72. The light deuterium water flow rate at the bottom of the enrichment cascade column-m 50 is metered by a flow meter 54.
The raw water of the final enrichment cascading tower-x is derived from the top product of the enrichment cascading tower-x-1. The raw water of the final enrichment cascading tower-m 50 is derived from the product at the top of the enrichment cascading tower-m-1. The electric heater 63 of the final enrichment cascade tower-m is electrified to work, and the bottom effusion is evaporated. The exhaust gas discharge shutoff valve 75 is opened, and the overhead evaporation gas is totally condensed in the condenser 66. The condensed liquid has two paths: (1) opening the shut-off valve 65 and allowing condensate to enter the food potable-grade light water storage sequence 72; (2) the rest condensate is returned to the final enrichment cascade column-x as reflux liquid. The cold source of the condenser 66 is normal-temperature industrial water, and the normal-temperature industrial water enters the raw material water tank 3 after exiting the condenser.
The product collected from the apparatus of the present invention is ultimately collected into a food and beverage grade light water storage train 72. From stripping tower-I to stripping tower-n, there is a special product collection tank 83, 84, etc.; from the enrichment column-I to the enrichment column-x, the rest of the enrichment columns have two product collection tanks 86, 87, 88, 89, etc., except for the enrichment column-I which has only one product collection tank 85.
Further, the cut-off valve 77 is opened, the stripping column-I top product is collected in the product collection tank 83, the cut-off valve 78 is opened, the stripping column-n top product is collected in the product collection tank 84, the cut-off valve 79 is opened, the enrichment column-I top product is collected in the product collection tank 85, the cut-off valve 80 is opened, the enrichment column-m top product is collected in the product collection tank 86, the cut-off valve 81 is opened, and the enrichment column-x top product is collected in the product collection tank 87. Opening the stop valve 82, and collecting light deuterium water at the bottom of the enrichment cascade tower-m into a product collection tank 88; the shut-off valve 121 is opened and the light deuterium depleted water at the bottom of the enrichment column-x is collected in the product collection tank 89.
The liquid discharged from the product collecting tanks at the tops of the stripping cascade tower-I-stripping cascade tower-n, the enriching cascade tower-I-enriching cascade tower-x are divided into two paths: (1) and opening the stop valves 90 and 98, starting the water pump 99, and stripping the top product of the cascade tower-I to the next-stage rectifying tower to serve as raw materials. And opening the stop valves 91 and 98, starting the water pump 99, and stripping the top product of the cascade tower-n to the next-stage rectifying tower to be used as raw materials. And opening stop valves 92 and 98, starting a water pump 99, and enriching the tower top product of the cascade tower-I to the next stage of rectifying tower to be used as raw materials. And opening stop valves 93 and 98, starting a water pump 99, and enriching the tower top product of the cascade tower-m to the next stage of rectifying tower to be used as raw materials. Opening stop valves 94 and 98, starting a water pump 99, and feeding the product at the top of the enrichment cascade tower-x to the next-stage rectifying tower to be used as a raw material; (2) opening a stop valve 100, enabling the product at the top of the stripping cascade tower-I to enter a water tank 106, opening stop valves 109 and 114, mixing the product at the top of the stripping cascade tower-I with high-concentration mineral solution, adding minerals into the product, and entering a water purification tank 115; opening a stop valve 101, feeding the product at the top of the stripping cascade tower-n into a water tank 106, opening stop valves 109 and 114, mixing the product at the top of the stripping cascade tower-I with high-concentration mineral solution, adding minerals into the product, and feeding the product into a water purification tank 115; opening a stop valve 102, feeding the product at the top of the enrichment cascade tower-I into a water tank 107, opening stop valves 110 and 113, mixing the product at the top of the enrichment cascade tower-I with a high-concentration mineral solution, adding minerals into the product, and feeding the product into a water purification tank 116; opening a stop valve 103, enabling the product at the top of the enrichment cascading tower-m to enter a water tank 107, opening stop valves 110 and 113, mixing the product at the top of the enrichment cascading tower-m with high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank 116; opening a stop valve 104, feeding the product at the top of the enrichment cascade tower-x into a water tank 107, opening stop valves 110 and 113, mixing the product at the top of the enrichment cascade tower-x with a high-concentration mineral solution, adding minerals into the product, and feeding the product into a water purification tank 116; the stop valve 105 is opened, the light deuterium water at the bottom of the enrichment cascade column-m enters the water tank 108, the stop valves 111 and 112 are opened, the light deuterium water at the bottom of the enrichment cascade column-m is mixed with the high-concentration mineral solution, mineral substances are added to the product, the mixture enters the water body purifying tank 119, the stop valve 122 is opened, the light deuterium water at the bottom of the enrichment cascade column-x enters the water tank 108, the stop valves 111 and 112 are opened, the light deuterium water at the bottom of the enrichment cascade column-x is mixed with the high-concentration mineral substance solution, mineral substances are added to the product, and the mixture enters the water body purifying tank 119.
The products at the bottom of the stripping cascade towers-I to-n realize UV sterilization in a water purifying tank 115, and a stop valve 117 is opened to output food drinking grade light water; the products at the bottoms of the enrichment cascade columns-I to-x realize UV sterilization in a water purification tank 116, and a stop valve 118 is opened to output food and drinking grade light water; the bottom product of the enrichment cascading tower except the enrichment cascading tower-I realizes UV sterilization in a water body purifying tank 119, and a stop valve 120 is opened to output food and drinking grade light water.
The invention relates to a technology and a device for producing food drinking grade light water, which are used for purifying and hardness-reducing (magnesium and calcium ion removal) industrial water as a production raw material of the food drinking grade light water and realize the industrial scale production of the food drinking grade light water by cascade vacuum rectification. The device adopts the cascade towers, and realizes the production of the light water with different abundance foods and drinking grades by arranging the regular towers and the bulk towers with different grades in series/parallel connection. The light water of the product can be used as food drinking grade light water by adding minerals, and can be directly drunk or used as raw material water of other functional beverages.
Claims (6)
1. A device for producing light water for food and drink is composed of at least stripping cascade tower system, enriching cascade tower system, storage system for light water for food and drink and vacuumizing system Four parts, characterized in that the stripping cascade tower system consists of a stripping cascade tower-I-stripping cascade tower-n which are connected in series, and the bottom of the stripping cascade tower is provided with reboiler heat source water for removing a large amount of deuterium water (D 2 O), the obtained product is used as a raw material source for enriching the food drinking grade light water, the enriching cascade tower system consists of an enriching cascade tower-I-enriching cascade tower-X, the top of the enriching cascade tower system is provided with condenser cold source water, the low-abundance food drinking grade light water at the top of the stripping cascade tower is used as a raw material, a random packing tower is used as a rectifying tower to produce high-abundance serial food drinking grade light water, and the food drinking grade light water storage system is used for completing the subsequent treatment of the product light water, including adding minerals beneficial to human bodies and carrying out UV disinfection on water bodies;
the inlet of the stripping cascade tower-I is connected with the overflow port of the stripping cascade tower-I (1), the liquid level at the bottom of the stripping cascade tower-I is connected with the outlet of the stripping cascade tower-I (1), the outlet of the stripping cascade tower-I is connected with the inlet of the cold end of a reboiler (9) respectively, the outlet of the cold end of the reboiler (9) is connected with the reboiling gas inlet at the bottom of the stripping cascade tower-I, the inlet of the hot end of the reboiler (9) is connected with the outlet of the cold end of a heat exchanger (12), the inlet of the cold end of the heat exchanger (12) is connected with cooling water, the inlet of the hot end of the heat exchanger (12) is connected with an industrial waste heat source, the outlet of the hot end is connected with the industrial waste discharge port, the inlet of the stop valve (13) and the inlet of the stop valve (10) are connected with the inlet of the stripping cascade tower-I, the outlet of the stop valve (13) is connected with the inlet of the class I heavy deuterium water collecting tank (15), a flowmeter (14) is arranged at the inlet of the class I heavy deuterium collecting tank (15), the raw material inlet (Pn-1) is connected with the light water storage sequence (72) of food drinking water, and the outlet of the stripping cascade tower (24) is connected with the discharge port (34) through the discharge port at the top of the discharge buffer tank (31; the outlet of the exhaust gas discharging buffer tank (34) is connected with the hot end inlet of the stripping cascade tower-n condenser (33), the hot end outlet of the condenser (33) is connected with the inlet of the condensed reflux buffer tank (32) through a confluence stop valve (35), the outlet of the condensed reflux buffer tank (32) is connected with the inlet of the reflux damper (30), the outlet of the reflux damper (30) is connected with the reflux inlet of the stripping cascade tower-n (24), the cold end inlet of the condenser (33) is connected with the cold end outlet of the condenser (36), the cold end outlet of the condenser (33) is connected with the cooling water inlet of the raw material water tank (3) through a cooling water inlet stop valve (4), the cold end inlet of the condenser (36) is connected with an industrial tap water pipe network, and the hot end inlet of the condenser (36) is respectively connected with the hot end outlet of the condenser (33) and the confluence stop valve (35); the hot end outlet of the condenser (36) is connected with the inlet of the food drinking grade light water storage sequence (72); the bottom liquid outlet of the enrichment cascade tower-I is connected with the inlet of a stop valve (40), the outlet of the stop valve (40) is connected with the inlet of a class I light deuterium water collection tank (42), a flowmeter (41) is arranged at the inlet of the class I light deuterium water collection tank (42), the raw material inlet (Prm-1) of the enrichment cascade tower-m (50) is connected with the raw material outlet of a food drinking grade light water storage sequence (72), and the top exhaust outlet of the enrichment cascade tower-m (50) is connected with the inlet of an exhaust gas emission buffer tank (57) through an exhaust gas emission stop valve (56); the outlet of the exhaust gas discharging buffer tank (57) is connected with the hot end inlet of the enrichment cascade tower-m condenser (58), the hot end outlet of the condenser (58) is connected with the inlet of the condensation reflux buffer tank (60) through a confluence stop valve (59), the outlet of the condensation reflux buffer tank (60) is connected with the inlet of the reflux damper (55), the outlet of the reflux damper (55) is connected with the reflux inlet of the enrichment cascade tower-m (50), the cold end inlet of the condenser (58) is connected with the cold end outlet of the condenser (61), the cold end outlet of the condenser (58) is connected with the cooling water inlet of the raw material water tank (3) through a cooling water inlet stop valve (4), the cold end inlet of the condenser (61) is connected with the hot end outlet of the condenser (58) and the confluence stop valve (59) respectively; the hot end outlet of the condenser (61) is connected with the inlet of a food and drink grade light water storage sequence (72), the liquid outlet at the bottom of the enrichment cascade tower-m is connected with the inlet of a stop valve (53), the outlet of the stop valve (53) is connected with the inlet of an m-class light deuterium water collection tank (67), a flowmeter (54) is arranged at the inlet of the m-class light deuterium water collection tank (67), the hot end outlet of the reboiler (9) and the hot end outlet of the reboiler (26) are connected with the inlet of a raw material pump (11), and the outlet of the raw material pump (11) is connected with the inlet of a raw material water tank (3) through a stop valve (108).
2. The device for producing the food drinking grade light water according to claim 1, wherein raw materials required by the food drinking grade light water storage system are raw material water tanks (3), the outlets of the raw material water tanks (3) are connected with the inlets of raw material outlet stop valves (5), the outlets of the raw material outlet stop valves (5) are connected with the inlets of raw material water softening tanks (6), the outlets of the raw material water softening tanks (6) are connected with the inlets of raw material buffer tanks (7), the raw material buffer tanks (7) are connected with the raw material inlets of a stripping cascade tower-I (1) through stop valves (8), and the top exhaust ports of the stripping cascade tower-I (1) are connected with the inlets of an exhaust gas emission buffer tank (18) through exhaust gas emission stop valves (16); the outlet of the exhaust gas discharging buffer tank (18) is connected with the hot end inlet of the stripping cascade tower-I condenser (20), the hot end outlet of the condenser (20) is connected with the inlet of the condensation reflux buffer tank (22) through the confluence stop valve (21), the outlet of the condensation reflux buffer tank (22) is connected with the inlet of the reflux damper (17), the outlet of the reflux damper (17) is connected with the reflux inlet of the stripping cascade tower-I (1), the cold end inlet of the condenser (20) is connected with the cold end outlet of the condenser (23), the cold end outlet of the condenser (20) is connected with the cooling water inlet of the raw material water tank (3) through the cooling water inlet stop valve (4), the cold end inlet of the condenser (23) is connected with the industrial tap water pipe network, and the hot end inlet of the condenser (23) is respectively connected with the hot end outlet of the condenser (20) and the confluence stop valve (21); the hot end outlet of the condenser (23) is connected with the inlet of the food and drink grade light water storage sequence (72).
3. The device for producing the light water of the food and drink grade according to claim 1, wherein an inlet of a liquid level communication stop valve (25) at the bottom of the stripping cascade tower-n is connected with an overflow port of the stripping cascade tower-n (24), an outlet of the liquid level communication stop valve (25) at the bottom of the stripping cascade tower-n and an outlet of a liquid outlet stop valve (73) at the bottom of the stripping cascade tower-n are respectively connected with a cold end inlet of a reboiler (26), the cold end outlet of the reboiler (26) is connected with a reboiling gas inlet at the bottom of the stripping cascade tower-n, a hot end inlet of the reboiler (26) is connected with a cold end outlet of a heat exchanger (12), an inlet of the stop valve (27) and an inlet of the stop valve (73) are jointly connected with a liquid outlet at the bottom of the stripping cascade tower-n, an outlet of the stop valve (27) is connected with an inlet of a heavy deuterium collection tank (29), a flowmeter (28) is arranged at the inlet of the heavy deuterium collection tank (29), a raw material inlet (Pdn) of the enriching cascade tower-I (37) is connected with a raw material inlet of a food grade light water storage sequence (72), and a top of the enriching cascade tower-I (37) is connected with a discharge buffer tank (45) through a discharge outlet (44) and a discharge outlet (45); the outlet of the exhaust gas discharging buffer tank (45) is connected with the hot end inlet of the enrichment cascade tower-I condenser (46), the hot end outlet of the condenser (46) is connected with the inlet of the condensation reflux buffer tank (47) through a confluence stop valve (48), the outlet of the condensation reflux buffer tank (47) is connected with the inlet of the reflux damper (43), the outlet of the reflux damper (43) is connected with the reflux inlet of the enrichment cascade tower-I (37), the cold end inlet of the condenser (46) is connected with the cold end outlet of the condenser (49), the cold end outlet of the condenser (46) is connected with the cooling water inlet of the raw material water tank (3) through a cooling water inlet stop valve (4), the cold end inlet of the condenser (49) is connected with the industrial tap water pipe network, and the hot end inlet of the condenser (49) is respectively connected with the hot end outlet of the condenser (46) and the confluence stop valve (48); the hot end outlet of the condenser (49) is connected with the inlet of the food drinking grade light water storage sequence (72).
4. The device for producing the food-grade drinking light water according to claim 1, wherein a raw material inlet (Prx-1) of the enrichment cascading tower-x (62) is connected with a raw material outlet of the food-grade drinking light water storage sequence (72), a top exhaust port of the enrichment cascading tower-x (62) is connected with a hot end inlet of an enrichment cascading tower-x condenser (66) through an exhaust gas discharge stop valve (75), a hot end outlet of the condenser (66) is respectively connected with a reflux liquid inlet of the enrichment cascading tower-x (62) and a stop valve (65), a stop valve (65) outlet is connected with a raw material inlet of the food-grade drinking light water storage sequence (72), a cold end inlet of the condenser (66) is connected with a tap water pipe network, a cold end outlet of the condenser (66) is connected with a cooling water inlet of the raw material water tank (3) through a cooling water inlet stop valve (4), a liquid outlet at the bottom of the enrichment cascading tower-x is connected with a stop valve (64) inlet, and the stop valve (64) outlet is connected with a reflux liquid inlet of the food-grade drinking light water storage sequence (72), and a flowmeter (74) is arranged on a flow path.
5. The device for producing the light water of the food and drink grade according to claim 1, wherein the heavy deuterium water collection tank (15) of class I of the stripping cascade tower-I, the heavy deuterium water collection tank (29) of class n of the stripping cascade tower-n, the light deuterium water collection tank (42) of class I of the enriching cascade tower-I are respectively connected with the inlet of the heavy deuterium water storage tank (68), the outlet of the heavy deuterium water storage tank (68) is discharged through a stop valve (69), and a system vacuumizing port is respectively arranged at the top of the exhaust gas discharge buffer tank (18), the top of the exhaust gas discharge buffer tank (34), the top of the exhaust gas discharge buffer tank (45), the top of the exhaust gas discharge buffer tank (57) and the outlet of the exhaust gas discharge stop valve (75).
6. A method of using the food and beverage grade light water production apparatus of any one of claims 1-5, comprising:
step 1: controlling the rectification operation pressure in all device towers to be 200-250 mmHg, vacuumizing the whole device by using a rotary vane vacuum pump (76) before the device is started, setting system vacuumizing ports V1-V5 at the top exhaust gas discharge stop valves (16, 31, 44, 56 and 75) of the stripping cascade tower-I-stripping cascade tower-n and the enrichment cascade tower-I-enrichment cascade tower-x, opening the exhaust gas discharge stop valves (16, 31, 44, 56 and 75), the raw material outlet stop valves (5), the cooling water inlet stop valves (4) and the stop valves (8, 13, 27, 40, 53 and 64), opening the stop valves (77-82 and 121), the stop valves (90-94), the stop valves (100-105 and 122) and the stop valves (109-111), and stopping vacuumizing when the pressure near the vacuum pumping ports is lower than 5KPa, and re-closing the valves to ensure that all the valves are in a closed state;
step 2: after the hardness of raw material water is reduced and impurities are removed through a raw material water softening tank (6), the raw material water enters a raw material buffer tank (7), a stop valve (8) is opened, the raw material water enters a stripping cascade tower-I (1), a stop valve (10) is opened, liquid accumulation at the bottom of the stripping cascade tower-I is evaporated, then an exhaust gas discharge stop valve (16) is opened, the evaporated gas is partially condensed in a condenser (20), and a gas-liquid mixture is provided with two paths: (1) opening a confluence stop valve (21), enabling condensate to enter a condensed reflux buffer tank (22) as reflux liquid, and arranging reflux damping (17) at a reflux liquid port for enabling reflux liquid of each parallel-connected tubular tower in the stripping cascade tower-I to be consistent; (2) the non-condensed water vapor enters a condenser (23), and enters a food drinking grade light water storage sequence (72) as a product sequence after condensation, cold sources of the condensers (20, 23) are normal temperature industrial water, a cooling water inlet stop valve (4) is opened, the normal temperature industrial water enters a raw material water tank (3), heavy deuterium water at the bottom of a rectifying byproduct stripping cascade tower-I (1) is introduced into a class I heavy deuterium water collecting tank (15) through a stop valve (13) which is opened, and then is collected into a heavy deuterium water storage tank (68), heavy deuterium water flow at the bottom of the stripping cascade tower-I (1) is metered through a flowmeter (14), and in order to maintain the liquid level of the accumulated liquid at the bottom of the stripping cascade tower-I (1) stable, a liquid level communication stop valve (2) at the bottom of the stripping cascade tower-I (1) is opened, and water overflowing to a specified liquid level can be introduced into a reboiler (9);
Step 3: the operation process of each stage of stripping cascade tower is similar to that of the stripping cascade tower-I (1), starting from the stripping cascade tower-II, each stage of raw water is from the product at the top of the previous stage, the raw water of the stripping cascade tower-n (24) is from the product at the top of the stripping cascade tower-n-1, a stop valve (73) is opened, liquid accumulation at the bottom of the stripping cascade tower-n (24) is evaporated, then an exhaust gas discharge stop valve (31) is opened, the evaporated gas is partially condensed in a condenser (33), and a gas-liquid mixture has two paths: (1) opening a confluence stop valve (35), enabling condensate to enter a condensed reflux buffer tank (33) as reflux liquid, and arranging reflux damping (30) at a reflux liquid port for enabling reflux liquid of each parallel-connected tubular tower in the stripping cascade tower-n to be consistent; (2) the vapor of the uncondensed water enters a condenser (36), and enters a food drinking grade light water storage sequence (72) as a product sequence after condensation, cold sources of the condensers (30, 33) are normal-temperature industrial water, and the normal-temperature industrial water enters a raw material water tank (3) after exiting the condenser;
step 4: the heavy deuterium water at the bottom of the stripping cascade tower-n (24) is introduced into an n-type heavy deuterium water collecting tank (29) through opening a stop valve (27), then is collected into a heavy deuterium water storage tank (68), the heavy deuterium water flow at the bottom of the stripping cascade tower-n (24) is metered by a flowmeter (27), and in order to maintain the stable liquid level of the liquid accumulation at the bottom of the stripping cascade tower-n (24) similar to other stripping cascade towers, the stop valve (25) is opened to ensure that the liquid level at the bottom of the stripping cascade tower-n (24) is communicated, water overflowing a specified liquid level can be introduced into a reboiler (26), the heat source of the reboiler at the bottom of the stripping cascade tower is derived from industrial waste heat, the industrial water exchanges heat with the boiled water in a heat exchanger (12), so that the boiled water absorbs the industrial waste heat as a reboiler heat source, the stop valve (108) is opened, and the boiled water discharged from the reboiler is introduced into a raw material water tank (3) through a water pump (11);
Step 5: the product at the top of the stripping cascade tower-n (24) is used as the raw material of an enrichment cascade tower-I (37), an electric heater (38) of the enrichment cascade tower-I is electrified to work, liquid is accumulated at the bottom of an evaporation tower, an exhaust gas discharge stop valve (44) is opened, the evaporated gas at the top of the tower is partially condensed in a condenser (46), and a gas-liquid mixture has two paths: (1) opening a confluence stop valve (48), enabling condensate to enter a condensed reflux buffer tank (47) as reflux liquid, and arranging reflux damping (43) at a reflux liquid port for enabling reflux liquid of each parallel tubular tower in the enrichment cascade tower-I (37) to be consistent; (2) the non-condensed water vapor enters a condenser (49), and enters a food drinking grade light water storage sequence (72) as a product sequence after condensation, cold sources of the condensers (46, 49) are normal-temperature industrial water, and the normal-temperature industrial water enters a raw material water tank (3) after exiting the condenser;
step 6: the heavy deuterium water at the bottom of the enrichment cascade tower-I (37) is led into a class I heavy deuterium water collection tank (42) through opening a stop valve (40), then is collected into a heavy deuterium water storage tank (68), the heavy deuterium water flow at the bottom of the enrichment cascade tower-I (37) is metered through a flowmeter (41), the operation process of each enrichment cascade tower is similar to that of the enrichment cascade tower-I (37), starting from the enrichment cascade tower-II, each level of raw material water is derived from a product at the top of the previous level, the raw material water of the enrichment cascade tower-m (50) is derived from a product at the top of the enrichment cascade tower-m-1, an electric heater (52) of the enrichment cascade tower-m is electrified, liquid at the bottom of an evaporation tower is evaporated, an exhaust gas discharge stop valve (56) is opened, the evaporated gas at the top of the evaporation gas at the bottom of the condenser (58) is partially condensed, and a gas-liquid mixture has two paths: (1) opening a confluence stop valve (59), enabling condensate to enter a condensed reflux buffer tank (60) as reflux liquid, and arranging reflux damping (55) at a reflux liquid port for enabling reflux liquid of each parallel tubular tower in the enrichment cascade tower-m (50) to be consistent; (2) the non-condensed water vapor enters a condenser (61), and enters a food drinking grade light water storage sequence (72) as a product sequence after condensation, cold sources of the condensers (58, 61) are normal-temperature industrial water, and the normal-temperature industrial water enters a raw material water tank (3) after exiting the condenser;
Step 7: starting from a rectifying tower behind the enrichment cascade tower-I, the bottom effusion is not collected to a heavy deuterium water storage tank (68) any more, but is used as a product sequence of food and drink grade light water, the light deuterium water at the bottom of the rectification byproduct enrichment cascade tower-m (50) is introduced into an m-class light deuterium water collection tank (67) through opening a stop valve (53), then enters a food and drink grade light water storage sequence (72), the light deuterium water at the bottom of the enrichment cascade tower-m (50) is metered through a flowmeter (54), the raw water of the final enrichment cascade tower-x is sourced from the product at the top of the enrichment cascade tower-x-1, the raw water of the final enrichment cascade tower-x (62) is sourced from the product at the top of the enrichment cascade tower-x-1, a final enrichment cascade tower-x electric heater (63) is electrified to work, the bottom effusion is evaporated, an exhaust gas discharge stop valve (75) is opened, all evaporated at the top of the tower in a condenser (66), and the condensed liquid has two paths: (1) opening a shut-off valve (65), the condensate entering a food drinking grade light water storage sequence (72); (2) the rest condensate is used as reflux liquid to return to the final-stage enrichment cascade tower-x, the cold source of the condenser (66) is normal-temperature industrial water, the normal-temperature industrial water enters the raw material water tank (3) after exiting the condenser, the product collected from the device of the invention is finally collected to a food drinking-stage light water storage sequence (72), and a special product collection tank (83, 84) is arranged from the stripping cascade tower-I to the stripping cascade tower-n; from the enrichment cascade column-I to the enrichment cascade column-x, except for the enrichment cascade column-I which has only one product collection tank (85), the rest of the enrichment cascade columns have two product collection tanks (86, 87, 88, 89);
Step 8: opening a stop valve (77), collecting the top product of the stripping cascade tower-I into a product collecting tank (83), opening a stop valve (78), collecting the top product of the stripping cascade tower-n into a product collecting tank (84), opening a stop valve (79), collecting the top product of the enrichment cascade tower-I into a product collecting tank (85), opening a stop valve (80), collecting the top product of the enrichment cascade tower-m into a product collecting tank (86), opening a stop valve (81), collecting the top product of the enrichment cascade tower-x into a product collecting tank (87), opening a stop valve (82), and collecting light deuterium water at the bottom of the enrichment cascade tower-m into a product collecting tank (88); the stop valve (121) is opened, light deuterium water at the bottom of the enrichment cascade tower-x is collected into the product collection tank (89), and the liquid discharged from the product collection tanks at the tops of the stripping cascade towers-I-stripping cascade tower-n, the enrichment cascade tower-I-enrichment cascade tower-x are divided into two paths: (1) opening stop valves (90, 98), opening a water pump (99), stripping the product at the top of the cascade tower-I to remove the next-stage rectifying tower to serve as raw materials, opening stop valves (91, 98), opening the water pump (99), stripping the product at the top of the cascade tower-n to remove the next-stage rectifying tower to serve as raw materials, opening the stop valves (92, 98), opening the water pump (99), enriching the product at the top of the cascade tower-I to remove the next-stage rectifying tower to serve as raw materials, opening the stop valves (93, 98), opening the water pump (99), enriching the product at the top of the cascade tower-m to remove the next-stage rectifying tower to serve as raw materials, opening the stop valves (94, 98), and opening the water pump (99), enriching the product at the top of the cascade tower-x to remove the next-stage rectifying tower to serve as raw materials; (2) opening a stop valve (100), enabling the top product of the stripping cascade tower-I to enter a water tank (106), opening stop valves (109, 114), mixing the top product of the stripping cascade tower-I with a high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank (115); opening a stop valve (101), enabling the product at the top of the stripping cascade tower-n to enter a water tank (106), opening stop valves (109, 114), mixing the product at the top of the stripping cascade tower-n with a high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank (115); opening a stop valve (102), feeding the product at the top of the enrichment cascade tower-I into a water tank (107), opening stop valves (110, 113), mixing the product at the top of the enrichment cascade tower-I with a high-concentration mineral solution, adding minerals into the product, and feeding the product into a water body purifying tank (116); opening a stop valve (103), enabling the tower top product of the enrichment cascade tower-m to enter a water tank (107), opening stop valves (110, 113), mixing the tower top product of the enrichment cascade tower-m with a high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank (116); opening a stop valve (104), enabling the product at the top of the enrichment cascade tower-x to enter a water tank (107), opening stop valves (110, 113), mixing the product at the top of the enrichment cascade tower-x with a high-concentration mineral solution, adding minerals into the product, and entering a water body purifying tank (116); opening a stop valve (105), enabling light deuterium water at the bottom of the enrichment cascade tower-m to enter a water tank (108), opening stop valves (111, 112), enabling light deuterium water at the bottom of the enrichment cascade tower-m to be mixed with high-concentration mineral solution, adding mineral substances to products, and entering a water body purifying tank (119), opening a stop valve (122), enabling light deuterium water at the bottom of the enrichment cascade tower-x to enter the water tank (108), opening stop valves (111, 112), enabling light deuterium water at the bottom of the enrichment cascade tower-x to be mixed with high-concentration mineral solution, adding mineral substances to products, entering the water body purifying tank (119), enabling the stripping cascade tower-I-stripping cascade tower-n bottom products to realize UV sterilization in the water body purifying tank (115), and opening the stop valve (117) to output food drinking grade light water; the products at the bottom of the enrichment cascade tower-I to the enrichment cascade tower-x realize UV sterilization in a water purification tank (116), and a stop valve (118) is opened to output food drinking grade light water; and besides the enrichment cascading tower-I, the bottom products of the rest enrichment cascading towers realize UV sterilization in a water purification tank (119), and a stop valve (120) is opened to output food and drinking grade light water.
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| US9062333B2 (en) * | 2009-08-14 | 2015-06-23 | Environmental Quality Management Associates | Method and apparatus for transforming waste into fuel ethanol |
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| CN101108724A (en) * | 2006-07-20 | 2008-01-23 | 柯香文 | Manufacture method of extracting pure tritium from raw material of light water (heavy water) containing tritium |
| CN101224929A (en) * | 2008-01-17 | 2008-07-23 | 上海上善若水生物工程有限公司 | Device and method for producing drinking ultra-light water |
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