CN106669210B - Sodium chloride's methanol-water solution evaporation recovery system - Google Patents

Sodium chloride's methanol-water solution evaporation recovery system Download PDF

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CN106669210B
CN106669210B CN201611137471.2A CN201611137471A CN106669210B CN 106669210 B CN106669210 B CN 106669210B CN 201611137471 A CN201611137471 A CN 201611137471A CN 106669210 B CN106669210 B CN 106669210B
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effect
pipe
outlet
triple
inlet
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CN106669210A (en
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杨杰
尹璐
许亮
王晓克
孙利敏
孙孝天
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Jiangsu Maiande Energy Saving Evaporation Equipment Co ltd
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Jiangsu Maiande Energy Saving Evaporation Equipment Co ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/26—Multiple-effect evaporating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0059—General arrangements of crystallisation plant, e.g. flow sheets
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Abstract

The invention relates to a salt-containing organic solution evaporation and recovery system, which comprises a stock solution storage tank and a one-effect falling-film evaporator, wherein an outlet of the stock solution storage tank is connected with a one-effect feed liquid inlet at the lower part of the one-effect falling-film evaporator through a feed pump; the material separation port at the lower part of the first-effect falling-film evaporator is connected with the first-effect separator through a communicating pipe, the steam exhaust port of the first-effect separator at the top of the first-effect separator is connected with the steam exhaust pipe of the first-effect separator, the material liquid outlet of the first-effect separator at the bottom of the first-effect separator is connected with a material liquid descending pipe, the material liquid descending pipe of the first-effect separator is connected with the circulating liquid inlet of the first-effect evaporator at the top of the first-effect falling-film evaporator through a first-effect circulating pump and a first-effect circulating pipe, and the outlet of the first-effect circulating pump is further connected with a material liquid output pipe. The method can realize the joint recovery of the organic solvent and the salt, and has low energy consumption.

Description

Sodium chloride's methanol-water solution evaporation recovery system
Technical Field
The invention relates to a sodium chloride methanol aqueous solution evaporation and recovery system, which can be applied to the treatment of high-salt-content organic solution in the environmental protection industry and the recovery of organic solvent in the food and pharmaceutical industry, and belongs to the technical field of industrial water treatment.
Background
In the environmental protection and pharmaceutical industry, solution components are increasingly complex due to the diversity of the chemical industry, most of the solution components are high-salt and high-organic matters, a rectification process is mostly adopted in a mode of recovering an organic solvent, the organic solvent overflows after rectification separation, inorganic salt still remains in a tower kettle, and residual liquid needs to be periodically discharged from the tower kettle. A part of organic solvent can be carried in the residual liquid, so that loss is caused, and the recovery rate of the organic solvent is reduced; meanwhile, the inorganic salt is not recycled, so that the burden of subsequent treatment is increased. In addition, the distillation in the tower still requires a large amount of generated steam and high energy consumption.
Disclosure of Invention
The invention aims to overcome the problems in the prior art and provide a methanol aqueous solution evaporation and recovery system for sodium chloride, which can realize the joint recovery of methanol and sodium chloride and has low energy consumption.
In order to solve the technical problems, the sodium chloride methanol aqueous solution evaporation recovery system comprises a stock solution storage tank and a one-effect falling-film evaporator, wherein an outlet of the stock solution storage tank is connected with an inlet of a feed pump, the lower part of the one-effect falling-film evaporator is connected with a one-effect liquid descending pipe, a one-effect evaporator feed liquid inlet is formed in the middle of the one-effect liquid descending pipe, an outlet of the feed pump is connected with a one-effect liquid descending pipe at the lower part of the one-effect falling-film evaporator, a one-effect evaporator steam inlet at the upper part of a shell pass of the one-effect falling-film evaporator is connected with a raw steam pipe, and a one-effect evaporator condensate water outlet at the lower part of the shell pass of the one-effect falling-film evaporator is connected with an inlet of a condensate water tank through a one-effect condensate water pipe; the material separation mouth of an effect falling film evaporator lower part links to each other with an effect separator through communicating pipe, an effect separator steam vent at an effect separator top links to each other with an effect separator steam exhaust pipe, an effect separator feed liquid export of an effect separator bottom with an effect feed liquid down pipe links to each other, the lower extreme of an effect feed liquid down pipe links to each other with the entry of an effect circulating pump, an effect circulating pump's export links to each other through an effect circulating pipe and an effect evaporator circulating liquid entry at an effect falling film evaporator top, an effect circulating pump's export still is connected with an effect feed liquid output tube.
Compared with the prior art, the invention has the following beneficial effects: the preheated methanol aqueous solution stock solution of the sodium chloride enters a feed liquid inlet of a one-effect evaporator of the one-effect falling-film evaporator, flows downwards along a feed liquid descending pipe together with a one-effect concentrated solution at the bottom of the one-effect falling-film evaporator and a one-effect concentrated solution at the bottom of a one-effect separator, is pumped out by a one-effect circulating pump, and is sent to a circulating liquid inlet of the one-effect evaporator at the top of the one-effect falling-film evaporator through a one-effect circulating pipe; raw steam of 135 ℃ provided by a raw steam pipe enters a shell pass of the one-effect falling film evaporator from a steam inlet of the one-effect evaporator to heat one-effect circulating concentrated solution flowing down along the wall of the falling film evaporator, and one-effect steam condensate of 100 ℃ is discharged into a condensate water tank from a condensate water outlet of the one-effect evaporator and a one-effect condensate water pipe to be recycled; the heated first-effect concentrated solution enters a first-effect separator from a communicating pipe for separation, first-effect steam at 72 ℃ enters a first-effect separator steam exhaust pipe from a first-effect separator steam exhaust port, and the main component of the first-effect steam is organic solvent steam; the concentrated first effect concentrated solution enters a first effect circulating pump for circulation, and part of the first effect concentrated solution at the outlet of the first effect circulating pump is discharged from a first effect liquid output pipe. Through the evaporation and concentration of the one-effect falling-film evaporator, a large amount of methanol is evaporated, the concentration of a sodium chloride solution is improved, and conditions are provided for subsequent further concentration and separation.
As an improvement of the invention, the invention also comprises a double-effect falling-film evaporator, wherein the lower part of the double-effect falling-film evaporator is connected with a double-effect feed liquid descending pipe, the middle part of the double-effect feed liquid descending pipe is provided with a double-effect evaporator feed liquid inlet, the double-effect evaporator feed liquid inlet is connected with the outlet of the first-effect feed liquid output pipe, the outlet of the first-effect separator exhaust pipe is connected with a double-effect evaporator steam inlet at the upper part of the shell pass of the double-effect falling-film evaporator, and a double-effect evaporator condensate outlet at the lower part of the shell pass of the double-effect falling-film evaporator is connected with a double-effect condensate pipe; the material separation mouth of two effect falling film evaporator lower part passes through communicating pipe and links to each other with two effect separator, two effect separator steam vent at two effect separator tops links to each other with two effect separator exhaust pipe, two effect separator feed liquid export of two effect separator bottom with two effect feed liquid down tube links to each other, the lower extreme of two effect feed liquid down tube links to each other with the entry of two effect circulating pump, two effect circulating pump's export links to each other through two effect circulating pipe and two effect evaporator circulation liquid entry at two effect falling film evaporator tops, two effect circulating pump's export still is connected with two effect feed liquid output tubes. After the primary-effect concentrated solution with the sodium chloride content of 2-3 wt% and the temperature of 73 ℃ is discharged from the primary-effect feed liquid output pipe, the primary-effect concentrated solution, the secondary-effect concentrated solution at the bottom of the secondary-effect falling film evaporator and the secondary-effect concentrated solution at the bottom of the secondary-effect separator flow downwards along a secondary-effect feed liquid descending pipe together, are pumped out by a secondary-effect circulating pump and are sent to a secondary-effect evaporator circulating liquid inlet at the top of the secondary-effect falling film evaporator through a secondary-effect circulating pipe; the 72 ℃ first-effect steam generated by the first-effect separator is mainly methanol steam and also contains partial water steam, the first-effect steam enters the shell pass of the double-effect falling film evaporator from the steam inlet of the double-effect evaporator after being discharged from the steam discharge pipe of the first-effect separator, the double-effect circulating concentrated solution flowing down along the wall of the falling film pipe is heated, and 72 ℃ double-effect condensate is discharged from a condensate outlet of the double-effect evaporator and a double-effect condensate pipe; the heated double-effect concentrated solution enters a double-effect separator from a communicating pipe for separation, the methanol and the water are continuously evaporated into double-effect steam, and the double-effect steam at 66 ℃ enters a steam exhaust pipe of the double-effect separator from a steam exhaust port of the double-effect separator; and (3) circulating the concentrated double-effect concentrated solution in a double-effect circulating pump, wherein part of the double-effect concentrated solution with the sodium chloride content of 4-6 wt% and the temperature of 68 ℃ is discharged from a double-effect feed liquid output pipe. The dual-effect falling-film evaporator further concentrates the primary-effect concentrated solution by using the primary-effect steam generated by the primary-effect separator, thereby not only recovering the waste heat generated by the primary-effect, but also further evaporating the methanol and improving the concentration of the sodium chloride solution.
As a further improvement of the invention, the invention also comprises a primary preheater, wherein the bottom outlet of the condensed water tank is connected with the inlet of a condensed water pump, the outlet of the condensed water pump is connected with the water inlet of the primary preheater through a condensed water supply pipe, the water outlet of the primary preheater is connected with a condensed water recovery pipe, the feed liquid inlet of the primary preheater is connected with the outlet of the feed pump, and the feed liquid outlet of the primary preheater is connected with the feed liquid inlet of the primary evaporator. The methanol water solution stock solution of sodium chloride enters a stock solution storage tank through a stock solution pipe, wherein the sodium chloride content is 1-1.5 wt%, and the temperature is 25 ℃; the primary steam condensate water at 98 ℃ is pumped out from a condensate water tank by a condensate water pump, enters a tube pass of a primary preheater to preheat a methanol aqueous solution stock solution of sodium chloride at a shell pass, so that the temperature of the stock solution is increased to 45 ℃, the temperature of the primary steam condensate water after heat release is 40 ℃, and the primary steam condensate water enters a condensate water recovery system through a condensate water recovery tube, thereby not only recovering the heat of the condensate water, but also reducing the load of a primary falling film evaporator and reducing the consumption of generated steam.
As a further improvement, the invention also comprises a secondary preheater, wherein a material liquid outlet of the primary preheater is connected with a material liquid inlet of the secondary preheater, and a material liquid outlet of the secondary preheater is connected with a material liquid inlet of the one-effect evaporator; and a secondary preheater steam inlet of the secondary preheater is connected with the steam generation pipe, and a secondary preheater condensate water outlet of the secondary preheater is connected with a water inlet of the condensate water tank through a high-temperature condensate water return pipe. The raw steam with the temperature of 135 ℃ enters the tube side of the secondary preheater to further heat the primary preheated stock solution, so that the temperature of the stock solution is continuously increased to 60 ℃, the 100 ℃ high-temperature condensate water after heat release enters the condensate water tank through the high-temperature condensate water return pipe and is sent to the primary preheater by the condensate water pump to further release heat, the temperature of the stock solution after the two-stage preheating is greatly increased, the load of the one-effect falling-film evaporator is greatly reduced, and the consumption of the raw steam is further reduced.
As a further improvement, the invention further comprises a triple-effect crystallizer, wherein a triple-effect crystallizer steam exhaust port is arranged at the top of the triple-effect crystallizer, a triple-effect crystallizer feed inlet, a triple-effect crystallizer circulation port and a triple-effect crystallizer return port are arranged in the middle of the circumferential wall of the triple-effect crystallizer, a triple-effect crystallizer discharge port is arranged at the bottom of the triple-effect crystallizer, and the triple-effect crystallizer feed inlet is connected with an outlet of the double-effect feed liquid output pipe; a triple-effect auxiliary heater is connected below the discharge port of the triple-effect crystallizer, the discharge port at the lower end of the triple-effect auxiliary heater is connected with the inlet of a triple-effect circulating pump through a triple-effect descending circulating pipe, the outlet of the triple-effect circulating pump is connected with the feed port at the lower end of the triple-effect heater through a triple-effect ascending circulating pipe, the discharge port at the upper end of the triple-effect heater is connected with the circulating port of the triple-effect crystallizer, and the outlet of the triple-effect circulating pump is also connected with a triple-effect crystal slurry output pipe; the exhaust port of the triple-effect crystallizer is connected with the exhaust pipe of the triple-effect crystallizer; the outlet of the steam exhaust pipe of the two-effect separator is connected with the steam inlet of the three-effect heater on the upper part of the shell pass of the three-effect heater, the outlet of the two-effect condensate pipe is connected with the three-effect condensate inlet on the lower part of the shell pass of the three-effect heater, and the three-effect condensate outlet on the lower part of the shell pass of the three-effect heater is connected with the three-effect condensate pipe; the outlet of the steam exhaust pipe of the two-effect separator is also connected with the steam inlet of the three-effect auxiliary heater on the upper part of the shell pass of the three-effect auxiliary heater, the outlet of the two-effect condensate pipe is also connected with the three-effect auxiliary condensate inlet on the lower part of the shell pass of the three-effect auxiliary heater, and the three-effect auxiliary condensate outlet on the lower part of the shell pass of the three-effect auxiliary heater is connected with the three-effect auxiliary condensate pipe. The falling film evaporator has the advantages of high heat transfer efficiency, small power of required matched power equipment and the like, but is not suitable for the evaporation of solution with solid particles or crystallized and separated out; the invention feeds the two-stage evaporation concentrated double-effect concentrated solution into a triple-effect crystallizer from a double-effect feed liquid output pipe through a feed inlet of the triple-effect crystallizer, the crystal slurry at the bottom of the triple-effect crystallizer is discharged from a discharge outlet of the triple-effect crystallizer and enters a triple-effect auxiliary heater for heating, the heated crystal slurry enters a triple-effect circulating pump along a triple-effect descending circulating pipe, then the crystal slurry ascends along a triple-effect ascending circulating pipe under the action of the triple-effect circulating pump and enters a triple-effect heater for further heating, the crystal slurry after reheating enters the triple-effect crystallizer from a circulating port of the triple-effect crystallizer, the moisture and the residual methanol are evaporated in large quantity, the sodium chloride is nearly saturated and crystallized and grows up in the triple-effect crystallizer, and the triple-effect steam at 60 ℃ generated by the triple-effect crystallizer is discharged from a steam outlet of the triple-effect crystallizer. And the 66 ℃ double-effect steam enters a triple-effect heater steam inlet at the upper part of the shell pass of the triple-effect heater and a triple-effect auxiliary heater steam inlet at the upper part of the shell pass of the triple-effect auxiliary heater from the outlet of the steam exhaust pipe of the double-effect separator respectively, and the heat of the double-effect steam is utilized to heat the triple-effect crystal slurry. After releasing heat in the triple-effect heater, methanol steam and water steam in the 66 ℃ double-effect steam are condensed into 66 ℃ triple-effect condensate, and the 66 ℃ triple-effect condensate is discharged into a triple-effect condensate pipe from a triple-effect condensate outlet; methanol steam and water vapor in the 66 ℃ secondary steam are condensed into 66 ℃ tertiary auxiliary condensate after releasing heat in the tertiary auxiliary heater, the 66 ℃ tertiary auxiliary condensate is discharged into a tertiary auxiliary condensate pipe from a tertiary auxiliary condensate outlet, and the secondary condensate entering from a tertiary auxiliary condensate inlet is also discharged into the tertiary auxiliary condensate pipe after being flashed and released heat in the tertiary auxiliary heater. In the triple-effect crystallizer, the circulation of the concentrated solution is forcibly pushed by a triple-effect circulating pump with larger power, the flow rate is high, the scaling is not easy to occur, and the triple-effect crystallizer is suitable for evaporating the solution separated by crystallization. According to the characteristics of the solution, the two-stage falling-film evaporator is adopted to concentrate the solution when the concentration of the inlet water is lower, so that the concentration of the solution is improved to a certain degree, and then the solution enters the three-effect crystallizer for evaporation and crystallization.
As a further improvement of the invention, the lower end of the triple-effect downward circulating pipe is also connected with an inlet of a triple-effect crystal slurry pump, an outlet of the triple-effect crystal slurry pump is connected with a feed inlet of a triple-effect swirler, a top outlet of the triple-effect swirler is connected with a reflux port of the triple-effect crystallizer through a triple-effect crystal slurry reflux pipe, a bottom outlet of the triple-effect swirler is connected with an inlet of a thick tank, a bottom outlet of the thick tank is connected with an upper feed inlet of a centrifuge, and a solid phase outlet of the centrifuge is connected with a salt collecting system; and a liquid phase outlet of the centrifuge and an overflow port of the thick tank at the upper part of the thick tank are respectively connected with an inlet of the mother liquid tank. The concentration of sodium chloride in the triple-effect crystal mush can reach 7-10% wt, the temperature is 66 ℃, part of the triple-effect crystal mush in the triple-effect downward circulating pipe is pumped out by a triple-effect crystal mush pump, the triple-effect crystal mush enters a feed inlet of a triple-effect swirler, after concentration, thickening and separation are carried out by the triple-effect swirler, a light phase enters a backflow port of a triple-effect crystallizer through a triple-effect crystal mush backflow pipe to circulate, a heavy phase enters a thickening tank to be further concentrated and crystallized, the concentration of sodium chloride after concentration and crystallization can reach 30-50% wt, the temperature is 55 ℃, then the light phase enters a centrifuge to be separated, the water content of the sodium chloride crystal is lower than 6% wt, the mother liquid of the centrifuge is discharged from a solid phase outlet of the centrifuge and enters a mother liquid tank to be collected, the mother liquid overflowing mother liquid at the upper part of the thickening tank also enters the mother tank to be collected, the sodium chloride concentration in the mother tank is lower than 30% wt, and the temperature is 45 ℃.
As a further improvement, the invention further comprises a four-effect crystallizer, wherein a four-effect crystallizer exhaust port is arranged at the top of the four-effect crystallizer, a four-effect crystallizer circulation port and a four-effect crystallizer return port are arranged in the middle of the circumferential wall of the four-effect crystallizer, and a four-effect crystallizer discharge port is arranged at the bottom of the four-effect crystallizer; a four-effect auxiliary heater is connected below the discharge port of the four-effect crystallizer, the discharge port at the lower end of the four-effect auxiliary heater is connected with the inlet of a four-effect circulating pump through a four-effect descending circulating pipe, the outlet of the four-effect circulating pump is connected with the feed port at the lower end of the four-effect heater through a four-effect ascending circulating pipe, and the discharge port at the upper end of the four-effect heater is connected with the circulating port of the four-effect crystallizer; the outlet of the triple-effect crystal slurry output pipe is connected with the four-effect downward circulating pipe, and the exhaust port of the four-effect crystallizer is connected with the exhaust pipe of the four-effect crystallizer; the outlet of the three-effect crystallizer steam exhaust pipe is connected with the shell side steam inlet of the four-effect heater on the upper part of the shell side of the four-effect heater, the outlet of the three-effect condensate pipe is connected with the condensate inlet of the four-effect heater on the lower end of the four-effect heater, and the condensate outlet of the four-effect heater on the lower part of the shell side of the four-effect heater is connected with the condensate pipe of the four-effect heater; the outlet of the three-effect crystallizer exhaust pipe is also connected with the inlet of a four-effect auxiliary heater on the upper part of the shell side of the four-effect auxiliary heater, the outlet of the three-effect auxiliary condensate pipe is connected with the condensate inlet of the four-effect auxiliary heater on the lower end of the four-effect auxiliary heater, and the condensate outlet of the four-effect auxiliary heater on the lower part of the shell side of the four-effect auxiliary heater is connected with the four-effect condensate pipe; the outlet of the four-effect condensate pipe is connected to the inlet of the solvent tank, the bottom of the solvent tank is connected with the inlet of the solvent pump, and the outlet of the solvent pump is connected with the solvent output pipe. Mother liquor collected by a mother liquor tank is sent into a feed inlet of a four-effect crystallizer of the four-effect crystallizer through a mother liquor return pipe by a mother liquor pump, crystal slurry at the bottom of the four-effect crystallizer is discharged from a discharge port of the four-effect crystallizer and enters a four-effect auxiliary heater for heating, the heated crystal slurry enters a four-effect circulating pump along a four-effect descending circulating pipe, three-effect crystal slurry flowing out of a three-effect crystal slurry output pipe also enters the four-effect circulating pump through the four-effect descending circulating pipe, the crystal slurry ascends along the four-effect ascending circulating pipe and enters the four-effect heater for further heating under the action of the four-effect circulating pump, the crystal slurry after being heated again enters the four-effect crystallizer from a circulation port of the four-effect crystallizer, moisture and residual methanol are evaporated in a large amount, sodium chloride is saturated in the four-effect crystallizer and crystallized to grow up, and 51 ℃ four-effect steam generated by the four-effect crystallizer is discharged from a steam discharge port of the four-effect crystallizer. The triple-effect steam enters a four-effect heater steam inlet on the upper part of the shell side of the four-effect heater and a four-effect auxiliary heater steam inlet on the upper part of the shell side of the four-effect auxiliary heater from an outlet of a triple-effect crystallizer steam exhaust pipe respectively, and the heat of the triple-effect steam is utilized to heat the four-effect magma. Methanol steam and water vapor in the triple-effect steam at 60 ℃ are condensed into quadruple-effect condensate at 60 ℃ after releasing heat in the quadruple-effect heater, the quadruple-effect condensate is discharged into the quadruple-effect condensate pipe from the quadruple-effect condensate outlet, and the triple-effect condensate entering from the quadruple-effect condensate inlet is also discharged into the quadruple-effect condensate pipe after being flashed and released heat in the quadruple-effect heater. After releasing heat in the four-effect auxiliary heater, methanol steam and water steam in the 60 ℃ triple-effect steam are condensed into 60 ℃ four-effect auxiliary condensate, the four-effect auxiliary condensate is discharged into a four-effect auxiliary condensate pipe from a four-effect auxiliary condensate outlet, and the triple-effect auxiliary condensate entering from a four-effect auxiliary condensate inlet is flashed in the four-effect auxiliary heater to release heat and is also discharged into the four-effect condensate pipe. And the methanol and the condensed water enter a solvent tank from a four-effect condensed liquid pipe, are pumped out by a solvent pump, enter a next procedure through a solvent output pipe, the temperature of the methanol and the water sent out by the solvent pump is 45 ℃, the concentration of the methanol is improved by 1-2% wt compared with the rectification, and the salt content in the methanol is lower than 0.05% wt.
As a further improvement of the invention, the lower end of the four-effect downward circulating pipe is also connected with an inlet of a four-effect crystal slurry pump, an outlet of the four-effect crystal slurry pump is connected with a feed inlet of a four-effect swirler, a top outlet of the four-effect swirler is connected with a return port of the four-effect crystallizer through a four-effect crystal slurry return pipe, and a bottom outlet of the four-effect swirler is connected with an inlet of the thickening tank; the outlet of the mother liquor tank is connected with the inlet of a mother liquor pump, and the outlet of the mother liquor pump is connected with a mother liquor filling port of the four-effect crystallizer in the middle of the circumferential wall of the four-effect crystallizer through a mother liquor return pipe. The concentration of sodium chloride in the four-effect magma can reach 25-30% wt, the temperature is 55 ℃, part of the four-effect magma in the four-effect downward circulating pipe is pumped out by a four-effect magma pump, enters a feed inlet of a four-effect swirler, is subjected to concentration, thickening and separation by the four-effect swirler, a light phase enters a return port of the four-effect crystallizer through a four-effect magma return pipe for circulation, a heavy phase enters a thickening tank for further concentration and crystal growing, then enters a centrifuge for separation, and sodium chloride crystals are discharged from a solid phase outlet of the centrifuge. The method can continuously separate sodium chloride while recovering the methanol, can reduce labor force by continuous operation, improves production efficiency, enables the sodium chloride and the methanol to be completely separated respectively, realizes zero emission, and realizes maximum environmental benefit and resource recycling. The invention adopts a multi-effect evaporation process, the secondary steam of the former effect is used as a heat source in the latter effect, and the evaporated condensate is used for preheating the raw materials, thereby greatly saving energy consumption and reducing operation cost.
As a further improvement of the invention, the outlet of the exhaust pipe of the four-effect crystallizer is connected with the air inlet at the upper end of the shell pass of the surface condenser, and the condensate outlet at the lower end of the shell pass of the surface condenser is connected with the inlet of the solvent tank through the return pipe of the surface condenser; the exhaust port at the lower end of the shell pass of the surface condenser is connected with a suction port of a water-ring vacuum pump, the exhaust port of the water-ring vacuum pump is connected with an exhaust pipe of the vacuum pump, a machine-sealed water outlet of the water-ring vacuum pump is connected with a circulating water tank of the vacuum pump, the bottom of the circulating water tank of the vacuum pump is connected with an inlet of a circulating water pump, and an outlet of the circulating water pump is connected with a machine-sealed water inlet of the water-ring vacuum pump. The method comprises the following steps that 51 ℃ four-effect steam enters a shell pass of a surface condenser from an outlet of a four-effect crystallizer steam exhaust pipe, cooling water is introduced into a pipe pass of the surface condenser to condense methanol steam and water steam in the four-effect steam into 40 ℃ four-effect condensate, the four-effect condensate enters a solvent tank through a surface condenser return pipe, non-condensable gas of the shell pass of the surface condenser is pumped out by a water ring vacuum pump, mechanical seal water of the water ring vacuum pump enters a vacuum pump circulating water tank, and the circulating water is pumped back to the water ring vacuum pump to realize closed circulation of the mechanical seal water, so that water consumption is reduced, and loss caused by the fact that the methanol is dissolved in the mechanical seal water of the water ring vacuum pump can be prevented.
As a further improvement of the invention, the tops of the stock solution storage tank and the solvent tank and the upper and lower parts of the shell pass of the two-effect falling-film evaporator, the three-effect heater, the three-effect auxiliary heater, the four-effect heater and the four-effect auxiliary heater are respectively provided with a non-condensable gas exhaust port, each non-condensable gas exhaust port is respectively connected with a non-condensable gas exhaust main pipe, and the outlet of the non-condensable gas exhaust main pipe is connected with the gas inlet at the upper end of the surface condenser; the top of the condensate water tank is connected with a condensate water tank steam exhaust pipe, and the outlet of the condensate water tank steam exhaust pipe and the exhaust port on the upper part and the lower part of the shell pass of the one-effect falling film evaporator are respectively connected with the steam inlet of the two-effect evaporator or the non-condensable gas exhaust main pipe. Non-condensable gas is dissolved in the solution, the non-condensable gas and steam generated by evaporation enter shell passes of the evaporators or the heaters during evaporation, and the heat transfer and mass transfer of the steam are affected if the non-condensable gas is accumulated in the shell passes because the non-condensable gas cannot be condensed, so that the heat transfer of the evaporators or the heaters is deteriorated. The invention pumps out the non-condensable gas at each position through the non-condensable gas exhaust main pipe, and the non-condensable gas is cooled by the surface condenser and then pumped out by the water ring vacuum pump, thereby improving the heat exchange efficiency of each evaporator or heater. When the system is just started, the exhaust ports at the upper part and the lower part of the shell pass of the one-effect falling film evaporator can be connected with the non-condensable gas exhaust main pipe, and the exhaust pipe of the condensate water tank is connected with the non-condensable gas exhaust main pipe, so that non-condensable gas can be extracted as soon as possible. When the system moves to a stable state, because the non-condensable gas temperature of the one-effect falling-film evaporator can reach 135 ℃, the non-condensable gas temperature of the condensate tank can reach 98 ℃, and a large amount of heat energy is contained, a valve between an exhaust port of the one-effect falling-film evaporator and a non-condensable gas exhaust main pipe is cut off, and a valve between the exhaust port of the one-effect falling-film evaporator and a steam inlet of the two-effect evaporator is opened; the valve between the steam exhaust pipe of the condensate water tank and the non-condensable gas exhaust main pipe is cut off, the valve between the steam exhaust pipe of the condensate water tank and the steam inlet of the two-effect evaporator is opened, so that the high-temperature first-effect non-condensable gas and the non-condensable gas of the condensate water tank enter the two-effect falling film evaporator to be discharged, and then the high-temperature first-effect non-condensable gas and the non-condensable gas of the condensate water tank are pumped out from the exhaust port of the two-effect evaporator through the non-condensable gas exhaust main pipe, so that heat in the high-temperature non-condensable gas can be recovered, and the load of the surface condenser can be reduced. The temperature of the non-condensable gas pumped by the shell pass of the two-effect falling-film evaporator is 72 ℃, the temperature of the non-condensable gas pumped by the solvent tank is 45 ℃, the temperature of the non-condensable gas pumped by the shell pass of the three-effect heater and the three-effect auxiliary heater is 66 ℃, the temperature of the non-condensable gas pumped by the shell pass of the four-effect heater and the four-effect auxiliary heater is 60 ℃, and the temperature of the non-condensable gas discharged by the exhaust port of the surface condenser is 51 ℃.
Drawings
The invention will be described in further detail with reference to the following drawings and detailed description, which are provided for reference and illustration purposes only and are not intended to limit the invention.
FIG. 1 shows a first embodiment of the sodium chloride methanol aqueous solution evaporation recovery system of the present invention.
FIG. 2 shows a second embodiment of the sodium chloride methanol aqueous solution evaporation recovery system of the present invention.
FIG. 3 shows a third embodiment of the sodium chloride methanol aqueous solution evaporation recovery system of the present invention.
In the figure: 1. a one-effect falling film evaporator; 1a, a feed liquid inlet of a one-effect evaporator; 1b, a material liquid descending pipe; 1c, a one-effect circulating pump; 1d, a circulating liquid inlet of the first-effect evaporator; 1e, a steam inlet of the one-effect evaporator; 1f, exhausting an exhaust port of the one-effect evaporator; 1g, a one-effect circulating pipe; 1h, a first effect liquid output pipe;
2. a first effect separator; 2a, a steam outlet of the single-effect separator; 2b, a feed liquid outlet of the first-effect separator; 2c, a steam exhaust pipe of the single-effect separator;
3. a dual-effect falling film evaporator; 3a, a feed liquid inlet of the double-effect evaporator; 3b, a secondary effect liquid descending pipe; 3c, a two-effect circulating pump; 3d, a circulating liquid inlet of the double-effect evaporator; 3e, a steam inlet of the double-effect evaporator; 3f, exhausting an exhaust port of the double-effect evaporator; 3g, a two-effect circulating pipe; a secondary effect feed liquid output pipe is used for 3 hours;
4. a two-effect separator; 4a, a steam outlet of the two-effect separator; 4b, a feed liquid outlet of the two-effect separator; 4c, a steam exhaust pipe of the two-effect separator;
5. a triple-effect crystallizer; 5a, a feed inlet of the triple-effect crystallizer; 5b, a steam outlet of the triple-effect crystallizer; 5c, a circulation port of the triple-effect crystallizer; 5d, a reflux port of the triple-effect crystallizer; 5e, discharging a discharge hole of the triple-effect crystallizer; 5f, a triple-effect downlink circulating pipe; 5g, a three-effect circulating pump; 5h, a triple-effect ascending circulating pipe; 5j, a triple-effect crystallizer exhaust pipe;
6. a triple effect heater; 6a, a steam inlet of the triple-effect heater; 6b, a triple effect condensate outlet; 6c, a triple effect condensate inlet;
7. a triple effect auxiliary heater; 7a, a steam inlet of the triple-effect auxiliary heater; 7b, a triple-effect auxiliary condensate outlet; 7c, a triple effect auxiliary condensate inlet;
8. a four-effect crystallizer; 8a, a four-effect crystallizer return port; 8b, a four-effect crystallizer steam outlet; 8c, a mother liquor injection port of the four-effect crystallizer; 8d, a four-effect crystallizer circulation port; 8e, discharging a discharge hole of the four-effect crystallizer; 8f, a four-effect downward circulating pipe; 8g, a four-effect circulating pump; 8h, a four-effect ascending circulating pipe; 8j, a four-effect crystallizer exhaust pipe;
9. a four-effect heater; 9a, a steam inlet of the four-effect heater; 9b, a condensate outlet of the four-effect heater; 9c, a condensate inlet of the four-effect heater;
10. a four-effect auxiliary heater; 10a, a steam inlet of the four-effect auxiliary heater; 10b, a condensate outlet of the four-effect auxiliary heater; 10c, a condensate inlet of the four-effect auxiliary heater;
11. thick tank; 11a, an overflow port of the thick tank;
12. a centrifuge; 12a, a centrifuge liquid phase outlet; 12b, a solid phase outlet of the centrifuge;
t1, stock solution storage tank; t2, condensing the water tank; t3, mother liquor tank; t4, a solvent tank; t5, circulating a water tank by using a vacuum pump;
B1. a feed pump; B2. a condensate pump; B3. a triple-effect crystal slurry pump; B4. a four-effect crystal slurry pump; B5. a solvent pump; B6. a mother liquor pump; B7. a water-ring vacuum pump; B8. a water circulating pump;
G1. a stock solution pipe; G2. a raw steam pipe; G3. a condensed water supply pipe; G4. a condensate recovery pipe; G5. a high-temperature condensed water return pipe; G6. a first effect condensate pipe; G7. a second-effect condensate pipe; G8. a triple-effect crystal slurry output pipe; G9. a triple effect condensate pipe; G10. a triple effect auxiliary condensate pipe; G11. a triple-effect crystal slurry return pipe; G12. a four-effect condensate pipe; G13. a four-effect crystal slurry return pipe; G14. a mother liquor return pipe; G15. a solvent output pipe; G16. a non-condensable gas exhaust main pipe; G17. a vacuum pump exhaust pipe;
H1. a primary preheater; H2. a secondary preheater; H3. a surface condenser;
s1, a three-effect swirler; s2, a four-effect swirler.
Detailed Description
As shown in fig. 1, the sodium chloride methanol aqueous solution evaporation recovery system of the present invention comprises a stock solution storage tank T1 and a one-effect falling-film evaporator 1, wherein an outlet of the stock solution storage tank T1 is connected with an inlet of a feed pump B1, a lower portion of the one-effect falling-film evaporator 1 is connected with a one-effect liquid descending pipe 1B, a middle portion of the one-effect liquid descending pipe 1B is provided with a one-effect evaporator liquid inlet 1a, an outlet of the feed pump B1 is connected with the one-effect liquid descending pipe 1B at a lower portion of the one-effect falling-film evaporator 1, a one-effect evaporator vapor inlet 1e at an upper portion of a shell pass of the one-effect falling-film evaporator is connected with a vapor generation pipe G2, and a one-effect evaporator condensate outlet at a lower portion of the shell pass of the one-effect falling-film evaporator is connected with an inlet of a condensate water tank T2 through a one-effect condensate pipe G6; a material separation port at the lower part of the one-effect falling-film evaporator 1 is connected with the one-effect separator 2 through a communicating pipe, a one-effect separator steam exhaust port 2a at the top of the one-effect separator 2 is connected with a one-effect separator steam exhaust pipe 2c, a one-effect separator material liquid outlet 2b at the bottom of the one-effect separator 2 is connected with a one-effect material liquid descending pipe 1b, the lower end of the one-effect material liquid descending pipe 1b is connected with an inlet of a one-effect circulating pump 1c, an outlet of the one-effect circulating pump 1c is connected with a one-effect evaporator circulating liquid inlet 1d at the top of the one-effect falling-film evaporator 1 through a one-effect circulating pipe 1g, and an outlet of the one-effect circulating pump 1c is also connected with an one-effect material liquid output pipe 1h.
A methanol aqueous solution stock solution of sodium chloride enters a stock solution storage tank T1 through a stock solution pipe G1, the content of sodium chloride is 1-1.5 wt%, the temperature is 25 ℃, the temperature is raised to 60 ℃ after preheating, the sodium chloride is sent into a feed solution inlet 1a of a one-effect evaporator of the one-effect falling-film evaporator 1 through a feed pump B1, and the sodium chloride, a one-effect concentrated solution at the bottom of the one-effect falling-film evaporator 1 and a one-effect concentrated solution at the bottom of a one-effect separator 2 flow downwards along a one-effect feed solution descending pipe 1B together and are pumped out by a one-effect circulating pump 1c and are sent to a one-effect evaporator circulating solution inlet 1d at the top of the one-effect falling-film evaporator 1 through a one-effect circulating pipe 1G; raw steam of 135 ℃ provided by a raw steam pipe G2 enters a shell pass of the one-effect falling-film evaporator 1 from a steam inlet 1e of the one-effect evaporator to heat a one-effect circulating concentrated solution flowing down along the wall of the falling-film tube, and one-effect steam condensate of 100 ℃ is discharged into a condensate water tank T2 from a condensate water outlet of the one-effect evaporator and a one-effect condensate water pipe G6 to be recycled; the heated first-effect concentrated solution enters a first-effect separator 2 from a communicating pipe for separation, first-effect steam at 72 ℃ enters a first-effect separator steam exhaust pipe 2c from a first-effect separator steam exhaust port 2a, and the main component of the first-effect steam is methanol steam; the concentrated first-effect concentrated solution enters a first-effect circulating pump 1c for circulation, and part of the first-effect concentrated solution at the outlet of the first-effect circulating pump 1c is discharged from a first-effect liquid output pipe 1h. Through the evaporation and concentration of the one-effect falling-film evaporator 1, a large amount of methanol is evaporated, the concentration of a sodium chloride solution is improved, and conditions are provided for subsequent further concentration and separation.
The sodium chloride methanol aqueous solution evaporation recovery system also comprises a double-effect falling-film evaporator 3, wherein the lower part of the double-effect falling-film evaporator 3 is connected with a double-effect feed liquid descending pipe 3b, the middle part of the double-effect feed liquid descending pipe 3b is provided with a double-effect evaporator feed liquid inlet 3a, the double-effect evaporator feed liquid inlet 3a is connected with the outlet of a first-effect feed liquid output pipe 1h, the outlet of a first-effect separator exhaust pipe 2c is connected with a double-effect evaporator steam inlet 3e at the upper part of the shell pass of the double-effect falling-film evaporator 3, and a double-effect evaporator condensate outlet at the lower part of the shell pass of the double-effect falling-film evaporator is connected with a double-effect condensate pipe G7; the material separation port at the lower part of the dual-effect falling-film evaporator 3 is connected with the dual-effect separator 4 through a communicating pipe, the steam exhaust port 4a of the dual-effect separator at the top of the dual-effect separator 4 is connected with the steam exhaust pipe 4c of the dual-effect separator, the feed liquid outlet 4b of the dual-effect separator at the bottom of the dual-effect separator 4 is connected with the dual-effect feed liquid descending pipe 3b, the lower end of the dual-effect feed liquid descending pipe 3b is connected with the inlet of the dual-effect circulating pump 3c, the outlet of the dual-effect circulating pump 3c is connected with the circulating liquid inlet 3d of the dual-effect evaporator at the top of the dual-effect falling-film evaporator 3 through the dual-effect circulating pipe 3g, and the outlet of the dual-effect circulating pump 3c is also connected with the dual-effect feed liquid output pipe 3h.
After the primary-effect concentrated solution with the sodium chloride content of 2-3 wt% and the temperature of 73 ℃ is discharged from the primary-effect feed liquid output pipe for 1h, the primary-effect concentrated solution, the secondary-effect concentrated solution at the bottom of the secondary-effect falling-film evaporator 3 and the secondary-effect concentrated solution at the bottom of the secondary-effect separator 4 flow downwards along a secondary-effect feed liquid descending pipe 3b together, are pumped out by a secondary-effect circulating pump 3c, and are sent to a secondary-effect evaporator circulating liquid inlet 3d at the top of the secondary-effect falling-film evaporator 3 through a secondary-effect circulating pipe 3 g; the first-effect steam generated by the first-effect separator 2 mainly contains methanol steam and part of water steam, the first-effect steam enters the shell pass of the double-effect falling film evaporator from the steam inlet 3e of the double-effect evaporator after being discharged from the steam discharge pipe 2c of the first-effect separator, the double-effect circulating concentrated solution flowing down along the wall of the falling film evaporator is heated, and the 72 ℃ double-effect condensate is discharged from a condensate outlet of the double-effect evaporator and a double-effect condensate pipe G7; the heated double-effect concentrated solution enters a double-effect separator 4 from a communicating pipe for separation, the methanol and the water are continuously evaporated into double-effect steam, and the double-effect steam at 66 ℃ enters a double-effect separator steam exhaust pipe 4c from a double-effect separator steam exhaust port 4 a; and (3) circulating the concentrated double-effect concentrated solution in a double-effect circulating pump 3c, wherein part of the double-effect concentrated solution with the sodium chloride content of 4-6 wt% and the temperature of 68 ℃ is discharged from a double-effect feed liquid output pipe for 3h. The dual-effect falling-film evaporator 3 utilizes the primary-effect steam generated by the primary-effect separator 2 to further concentrate the primary-effect concentrated solution, thereby not only recovering the waste heat generated by the primary effect, but also further evaporating the methanol and improving the concentration of the sodium chloride solution.
As shown in fig. 2, the sodium chloride methanol aqueous solution evaporation recovery system of the present invention further includes a primary preheater H1, the bottom outlet of the condensed water tank T2 is connected to the inlet of the condensed water pump B2, the outlet of the condensed water pump B2 is connected to the water inlet of the primary preheater H1 through a condensed water supply pipe G3, the water outlet of the primary preheater H1 is connected to the condensed water recovery pipe G4, the primary preheater feed liquid inlet of the primary preheater H1 is connected to the outlet of the feed pump B1, and the primary preheater feed liquid outlet of the primary preheater H1 is connected to the feed liquid inlet 1a of the primary evaporator.
The 98 ℃ primary steam condensate is pumped out from a condensate water tank T2 by a condensate water pump B2, enters a tube pass of a primary preheater H1 to preheat a methanol aqueous solution stock solution of sodium chloride on a shell pass, the temperature of the stock solution is increased to 45 ℃, the temperature of the released primary steam condensate is 40 ℃, and the released primary steam condensate enters a condensate water recovery system through a condensate water recovery tube G4, so that the heat of the condensate water is recovered, the load of the primary falling film evaporator 1 is reduced, and the consumption of generated steam is reduced.
As shown in fig. 3, the sodium chloride methanol aqueous solution evaporation recovery system of the present invention further comprises a secondary preheater H2, wherein a feed liquid outlet of the primary preheater is connected to a feed liquid inlet of the secondary preheater of H2, and a feed liquid outlet of the secondary preheater of H2 is connected to a feed liquid inlet 1a of the one-effect evaporator; the steam inlet of the secondary preheater H2 is connected with the raw steam pipe G2, and the condensed water outlet of the secondary preheater H2 is connected with the water inlet of the condensed water tank T2 through a high-temperature condensed water return pipe G5.
The raw steam with the temperature of 135 ℃ enters the tube pass of the secondary preheater H2 to further heat the primary preheated stock solution, so that the temperature of the stock solution is continuously increased to 60 ℃, the 100 ℃ high-temperature condensate water after heat release enters the condensate water tank T2 through the high-temperature condensate water return tube G5, and then is sent to the primary preheater H1 by the condensate water pump B2 to further release heat, the temperature of the stock solution is greatly increased after the two-stage preheating, the load of the one-effect falling-film evaporator 1 is greatly reduced, and the consumption of the raw steam is further reduced.
The sodium chloride methanol aqueous solution evaporation recovery system also comprises a triple-effect crystallizer 5, wherein a triple-effect crystallizer steam exhaust port 5b is arranged at the top of the triple-effect crystallizer 5, a triple-effect crystallizer feed inlet 5a, a triple-effect crystallizer circulation port 5c and a triple-effect crystallizer return port 5d are arranged in the middle of the circumferential wall of the triple-effect crystallizer 5, a triple-effect crystallizer discharge outlet 5e is arranged at the bottom of the triple-effect crystallizer 5, and the feed inlet 5a of the triple-effect crystallizer is connected with the outlet of a double-effect feed liquid output pipe 3 h; a triple-effect auxiliary heater 7 is connected below the discharge port 5e of the triple-effect crystallizer, the discharge port at the lower end of the triple-effect auxiliary heater 7 is connected with the inlet of a triple-effect circulating pump 5G through a triple-effect descending circulating pipe 5f, the outlet of the triple-effect circulating pump 5G is connected with the feed port at the lower end of the triple-effect heater 6 through a triple-effect ascending circulating pipe 5h, the discharge port at the upper end of the triple-effect heater 6 is connected with a circulation port 5c of the triple-effect crystallizer, and the outlet of the triple-effect circulating pump 5G is also connected with a triple-effect crystal slurry output pipe G8; the exhaust port 5b of the triple-effect crystallizer is connected with an exhaust pipe 5j of the triple-effect crystallizer.
The outlet of the steam exhaust pipe 4c of the two-effect separator is connected with the steam inlet 6a of the three-effect heater on the upper part of the shell pass of the three-effect heater 6, the outlet of the two-effect condensate pipe G7 is connected with the three-effect condensate inlet 6c on the lower part of the shell pass of the three-effect heater 6, and the three-effect condensate outlet 6b on the lower part of the shell pass of the three-effect heater 6 is connected with the three-effect condensate pipe G9; the outlet of the steam exhaust pipe 4c of the two-effect separator is also connected with the steam inlet 7a of the three-effect auxiliary heater on the upper part of the shell pass of the three-effect auxiliary heater 7, the outlet of the two-effect condensate pipe G7 is also connected with the three-effect auxiliary condensate inlet 7c on the lower part of the shell pass of the three-effect auxiliary heater 7, and the three-effect auxiliary condensate outlet 7b on the lower part of the shell pass of the three-effect auxiliary heater 7 is connected with the three-effect auxiliary condensate pipe G10.
The invention sends the two-stage evaporation concentrated double-effect concentrated solution into a triple-effect crystallizer 5 from a double-effect feed liquid output pipe 3h through a triple-effect crystallizer feed inlet 5a, the crystal mush at the bottom of the triple-effect crystallizer 5 is discharged from a triple-effect crystallizer discharge outlet 5e and enters a triple-effect auxiliary heater 7 to be heated, the heated crystal mush enters a triple-effect circulating pump 5g along a triple-effect descending circulating pipe 5f, then the crystal mush ascends along a triple-effect ascending circulating pipe 5h under the action of the triple-effect circulating pump 5g and enters a triple-effect heater 6 to be further heated, the crystal mush after being heated again enters the triple-effect crystallizer 5 from a triple-effect crystallizer circulating port 5c, the moisture and the residual methanol are evaporated in a large amount, the sodium chloride is nearly saturated and crystallized and grows up in the triple-effect crystallizer 5, and the triple-effect steam at 60 ℃ generated by the triple-effect crystallizer 5 is discharged from a triple-effect crystallizer steam outlet 5b. The 66 ℃ double-effect steam enters a triple-effect heater steam inlet 6a at the upper part of the shell pass of the triple-effect heater 6 and a triple-effect auxiliary heater steam inlet 7a at the upper part of the shell pass of the triple-effect auxiliary heater 7 from the outlet of the double-effect separator steam exhaust pipe 4c respectively, and the heat of the double-effect steam is utilized to heat the triple-effect magma.
After releasing heat in the triple-effect heater 6, methanol steam and water steam in the 66 ℃ double-effect steam are condensed into 66 ℃ triple-effect condensate, the triple-effect condensate is discharged into a triple-effect condensate pipe G9 from a triple-effect condensate outlet 6b, and the double-effect condensate entering from a triple-effect condensate inlet 6c is also discharged into a triple-effect condensate pipe G9 after being flashed and released heat in the triple-effect heater 6;
after releasing heat in the triple-effect auxiliary heater 7, methanol steam and water steam in the 66 ℃ double-effect steam are condensed into 66 ℃ triple-effect auxiliary condensate, the triple-effect auxiliary condensate is discharged into a triple-effect auxiliary condensate pipe G10 from a triple-effect auxiliary condensate outlet 7b, and the double-effect condensate entering from a triple-effect auxiliary condensate inlet 7c is flashed in the triple-effect auxiliary heater 7 to release heat, and then is also discharged into a triple-effect auxiliary condensate pipe G10.
The lower end of the triple-effect downward circulating pipe 5f is also connected with an inlet of a triple-effect crystal slurry pump B3, an outlet of a triple-effect crystal slurry pump B3 is connected with a feed inlet of a triple-effect swirler S1, a top outlet of the triple-effect swirler S1 is connected with a reflux port 5d of the triple-effect crystallizer through a triple-effect crystal slurry reflux pipe G11, a bottom outlet of a triple-effect swirler S1 is connected with an inlet of a thick tank 11, a bottom outlet of the thick tank 11 is connected with an upper feed inlet of a centrifuge 12, and a solid phase outlet 12B of the centrifuge 12 is connected with a salt collecting system; the centrifuge liquid phase outlet 12a of the centrifuge 12 and the thick tank overflow port 11a at the upper part of the thick tank 11 are respectively connected with the inlet of the mother liquid tank T3.
The concentration of sodium chloride in the triple-effect crystal slurry can reach 7-10% wt, the temperature is 66 ℃, part of the triple-effect crystal slurry in the triple-effect downward circulating pipe 5f is pumped out by a triple-effect crystal slurry pump B3, enters a feed inlet of a triple-effect swirler S1, is subjected to concentration, thickening and separation by a triple-effect swirler S1, a light phase enters a reflux port 5d of the triple-effect crystallizer through a triple-effect crystal slurry reflux pipe G11 for circulation, a heavy phase enters a thick tank 11 for further concentration and crystal cultivation, the concentration of sodium chloride after concentration and crystal cultivation can reach 30-50% wt, the temperature is 55 ℃, then the light phase enters a centrifuge 12 for separation, the water content of sodium chloride crystals is lower than 6% wt and is discharged from a solid phase outlet 12B of the centrifuge 12, mother liquor of the centrifuge is discharged from a liquid phase outlet 12a of the centrifuge 12 and enters a mother liquor tank T3 for collection, mother liquor overflowing from the upper part of the thick tank 11 also enters a mother liquor tank T3 for collection, and the concentration of sodium chloride in mother liquor T3 is lower than 30% wt, the temperature was 45 ℃.
The sodium chloride methanol aqueous solution evaporation recovery system also comprises a four-effect crystallizer 8, wherein a four-effect crystallizer steam exhaust port 8b is arranged at the top of the four-effect crystallizer 8, a four-effect crystallizer circulation port 8d and a four-effect crystallizer return port 8a are arranged in the middle of the circumferential wall of the four-effect crystallizer 8, and a four-effect crystallizer discharge port 8e is arranged at the bottom of the four-effect crystallizer 8; a four-effect auxiliary heater 10 is connected below the discharge port 8e of the four-effect crystallizer, the discharge port at the lower end of the four-effect auxiliary heater 10 is connected with the inlet of a four-effect circulating pump 8g through a four-effect descending circulating pipe 8f, the outlet of the four-effect circulating pump 8g is connected with the feed port at the lower end of a four-effect heater 9 through a four-effect ascending circulating pipe 8h, and the discharge port at the upper end of the four-effect heater 9 is connected with a circulation port 8d of the four-effect crystallizer; the outlet of the triple-effect crystal slurry output pipe G8 is connected with a four-effect downward circulating pipe 8f, and the exhaust port 8b of the four-effect crystallizer is connected with the exhaust pipe 8j of the four-effect crystallizer.
The outlet of the steam exhaust pipe 5j of the triple-effect crystallizer is connected with the shell side steam inlet of the four-effect heater at the upper part of the shell side of the four-effect heater 9, the outlet of a triple-effect condensate pipe G9 is connected with the condensate inlet 9c of the four-effect heater at the lower end of the four-effect heater 9, and the condensate outlet 9b of the four-effect heater at the lower part of the shell side of the four-effect heater 9 is connected with a four-effect condensate pipe G12; the outlet of the triple-effect crystallizer steam exhaust pipe 5j is also connected with a four-effect auxiliary heater steam inlet 10a at the upper part of the shell pass of the four-effect auxiliary heater 10, the outlet of a triple-effect auxiliary condensate pipe G10 is connected with a four-effect auxiliary heater condensate inlet 10c at the lower end of the four-effect auxiliary heater 10, and a four-effect auxiliary heater condensate outlet 10b at the lower part of the shell pass of the four-effect auxiliary heater is connected with a four-effect condensate pipe G12; the outlet of the four-effect liquid condensation pipe G12 is connected to the inlet of a solvent tank T4, the bottom of the solvent tank T4 is connected with the inlet of a solvent pump B5, and the outlet of the solvent pump B5 is connected with a solvent output pipe G15.
Mother liquor collected by a mother liquor tank T3 is sent into a feed inlet of the four-effect crystallizer 8 by a mother liquor pump B6 through a mother liquor return pipe G14, the crystal slurry at the bottom of the four-effect crystallizer 8 is discharged from a discharge port 8e of the four-effect crystallizer and enters a four-effect auxiliary heater 10 to be heated, the heated crystal slurry enters a four-effect circulating pump 8G along a four-effect downward circulating pipe 8f, the triple-effect crystal slurry flowing out of a triple-effect crystal slurry output pipe G8 enters the four-effect circulating pump 8G through the four-effect downward circulating pipe 8f, under the action of a four-effect circulating pump 8g, the crystal slurry ascends along a four-effect ascending circulating pipe 8h and enters a four-effect heater 9 for further heating, the crystal slurry after being heated again enters a four-effect crystallizer 8 from a four-effect crystallizer circulating port 8d, the water and the residual methanol are largely evaporated, the sodium chloride is saturated and crystallized to grow in the four-effect crystallizer 8, and the four-effect steam with the temperature of 51 ℃ generated by the four-effect crystallizer 8 is discharged from a steam outlet 8b of the four-effect crystallizer. The triple-effect steam enters a four-effect heater steam inlet 9a at the upper part of the shell pass of the four-effect heater 9 and a four-effect auxiliary heater steam inlet 10a at the upper part of the shell pass of the four-effect auxiliary heater 10 from the outlet of the triple-effect crystallizer steam exhaust pipe 5j respectively, and the heat of the triple-effect steam is utilized to heat the four-effect crystal slurry.
After releasing heat in the four-effect heater 9, methanol vapor and water vapor in the 60 ℃ triple-effect vapor are condensed into 60 ℃ four-effect condensate, the 60 ℃ four-effect condensate is discharged into a four-effect condensate pipe G12 from a four-effect condensate outlet, and the triple-effect condensate entering from a four-effect condensate inlet is also discharged into a four-effect condensate pipe G12 after being flashed and released heat in the four-effect heater 9.
After releasing heat in the four-effect auxiliary heater 10, methanol vapor and water vapor in the 60 ℃ triple-effect vapor are condensed into 60 ℃ four-effect auxiliary condensate, the 60 ℃ four-effect auxiliary condensate is discharged into a four-effect auxiliary condensate pipe from a four-effect auxiliary condensate outlet, and the triple-effect auxiliary condensate entering from a four-effect auxiliary condensate inlet is flashed in the four-effect auxiliary heater 10 to release heat, and then is also discharged into a four-effect condensate pipe G12.
Methanol and condensed water enter a solvent tank T4 from a four-effect condensed water pipe G12, are pumped out by a solvent pump B5 and enter a subsequent process through a solvent output pipe G15, the temperature of the methanol and the water sent out by the solvent pump B5 is 45 ℃, the concentration of the methanol is improved by 1-2 wt% compared with the rectification, and meanwhile, the salt content in the methanol is lower than 0.05 wt%.
The lower end of the four-effect downward circulating pipe 8f is also connected with the inlet of a four-effect crystal slurry pump B4, the outlet of a four-effect crystal slurry pump B4 is connected with the feed inlet of a four-effect swirler S2, the top outlet of the four-effect swirler S2 is connected with the return port 8a of the four-effect crystallizer through a four-effect crystal slurry return pipe G13, and the bottom outlet of the four-effect swirler S2 is connected with the inlet of the thick tank 11; the outlet of the mother liquor tank T3 is connected with the inlet of a mother liquor pump B6, and the outlet of a mother liquor pump B6 is connected with a mother liquor injection port 8c of the four-effect crystallizer in the middle of the circumferential wall of the four-effect crystallizer 8 through a mother liquor return pipe G14.
The concentration of sodium chloride in the four-effect magma can reach 25-30% wt, the temperature is 55 ℃, part of the four-effect magma in the four-effect downward circulating pipe 8f is pumped out by a four-effect magma pump B4, enters a feed inlet of a four-effect swirler S2, is concentrated, thickened and separated by a four-effect swirler S2, a light phase enters a return port 8a of the four-effect crystallizer through a four-effect magma return pipe G13 for circulation, a heavy phase enters a thickening tank 11 for further concentration and crystal cultivation, then enters a centrifuge 12 for separation, and sodium chloride crystals are discharged from a solid phase outlet of the centrifuge 12. The method can continuously separate sodium chloride while recovering the methanol, so that the sodium chloride and the methanol are completely separated respectively, and zero emission is realized. The secondary steam of the former effect is used as a heat source in the latter effect, and the evaporated condensate is used for preheating the raw materials, so that the energy consumption is greatly saved, and the operation cost is reduced.
An outlet of a four-effect crystallizer exhaust pipe 8j is connected with an air inlet at the upper end of the shell pass of the surface condenser H3, and a condensate discharge port at the lower end of the shell pass of the surface condenser H3 is connected with an inlet of a solvent tank T4 through a surface condenser return pipe; an exhaust port at the lower end of the shell side of the surface condenser H3 is connected with a suction port of a water-ring vacuum pump B7, an exhaust port of a water-ring vacuum pump B7 is connected with a vacuum pump exhaust pipe G17, a machine seal water outlet of the water-ring vacuum pump B7 is connected with a vacuum pump circulating water tank T5, the bottom of the vacuum pump circulating water tank T5 is connected with an inlet of a circulating water pump B8, and an outlet of the circulating water pump B8 is connected with a machine seal water inlet of a water-ring vacuum pump B7.
The method is characterized in that the 51 ℃ four-effect steam enters the shell pass of a surface condenser H3 from the outlet of a four-effect crystallizer exhaust pipe 8j, cooling water is introduced into the tube pass of a surface condenser H3 to condense methanol steam and water steam in the four-effect steam into 40 ℃ four-effect condensate, the four-effect condensate enters a solvent tank T4 through a surface condenser return pipe, non-condensable gas in the shell pass of the surface condenser H3 is pumped out by a water ring vacuum pump B7, machine seal water of the water ring vacuum pump B7 enters a vacuum pump circulating water tank T5, and the water ring vacuum pump B7 is returned by a circulating water pump B8 to realize closed circulation of the machine seal water, so that water consumption is reduced, and loss caused by the fact that the methanol is dissolved in the machine seal water of the water ring vacuum pump can be prevented.
The top of the stock solution storage tank T1 and the top of the solvent tank T4 and the upper and lower parts of the shell pass of the two-effect falling film evaporator 3, the three-effect heater 6, the three-effect auxiliary heater 7, the four-effect heater 9 and the four-effect auxiliary heater 10 are respectively provided with a non-condensable gas exhaust port, each non-condensable gas exhaust port is respectively connected with a non-condensable gas exhaust main pipe G16, and the outlet of the non-condensable gas exhaust main pipe G16 is connected with a gas inlet at the upper end of a surface condenser H3; the top of the condensate water tank T2 is connected with a condensate water tank steam exhaust pipe, and the outlet of the condensate water tank steam exhaust pipe and the exhaust port at the upper part and the lower part of the shell pass of the one-effect falling film evaporator are respectively connected with a steam inlet 3e of the two-effect evaporator or connected with a non-condensable gas exhaust header pipe G16.
In the invention, non-condensable gas at each part is pumped out through a non-condensable gas exhaust manifold G16, cooled by a surface condenser H3 and pumped out by a water ring vacuum pump B7, thereby improving the heat exchange efficiency of each evaporator or heater. When the system is just started, the exhaust ports at the upper part and the lower part of the shell pass of the one-effect falling-film evaporator can be connected with the non-condensable gas exhaust main pipe G16, and the exhaust pipe of the condensate tank is connected with the non-condensable gas exhaust main pipe G16, so that non-condensable gas can be extracted as soon as possible.
When the system moves to a stable state, because the non-condensable gas temperature of the one-effect falling-film evaporator 1 can reach 135 ℃, the non-condensable gas temperature of the condensed water tank T2 can reach 98 ℃, and a large amount of heat energy is accumulated, a valve between the exhaust port 1f of the one-effect evaporator of the one-effect falling-film evaporator 1 and the non-condensable gas exhaust header pipe G16 is cut off, and a valve between the exhaust port 1f of the one-effect evaporator and the steam inlet 3e of the two-effect evaporator is opened; and cutting off a valve between a steam exhaust pipe of the condensate water tank and the non-condensable gas exhaust main pipe G16, and opening a valve between the steam exhaust pipe of the condensate water tank and a steam inlet 3e of the two-effect evaporator, so that the high-temperature first-effect non-condensable gas and the non-condensable gas of the condensate water tank T2 enter the two-effect falling film evaporator 3 to release heat, and then the high-temperature first-effect non-condensable gas and the non-condensable gas are pumped out from an exhaust port 3f of the two-effect evaporator through the non-condensable gas exhaust main pipe G16, thereby not only recovering the heat in the high-temperature non-condensable gas, but also lightening the load of the surface condenser H3.
The temperature of the non-condensable gas extracted by the shell pass of the two-effect falling-film evaporator 3 is 72 ℃, the temperature of the non-condensable gas extracted by the solvent tank T4 is 45 ℃, the temperature of the non-condensable gas extracted by the shell passes of the three-effect heater 6 and the three-effect auxiliary heater 7 is 66 ℃, the temperature of the non-condensable gas extracted by the shell passes of the four-effect heater 9 and the four-effect auxiliary heater 10 is 60 ℃, and the temperature of the non-condensable gas discharged by the exhaust port of the surface condenser is 51 ℃.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention. In addition to the above embodiments, the present invention may have other embodiments, and any technical solutions formed by equivalent substitutions or equivalent transformations fall within the scope of the claims of the present invention. Technical features of the present invention which are not described may be implemented by or using the prior art, and will not be described herein.

Claims (8)

1. The utility model provides a methanol-water solution evaporation recovery system of sodium chloride, includes the stoste storage tank, the export of stoste storage tank links to each other with the entry of charge-in pump, its characterized in that: the device is characterized by further comprising a first-effect falling-film evaporator, a second-effect falling-film evaporator and a third-effect crystallizer, wherein the lower part of the first-effect falling-film evaporator is connected with a first-effect feed liquid descending pipe, the middle part of the first-effect feed liquid descending pipe is provided with a first-effect evaporator feed liquid inlet, the outlet of a feed pump is connected with the first-effect feed liquid descending pipe at the lower part of the first-effect falling-film evaporator, a first-effect evaporator steam inlet at the upper part of a shell pass of the first-effect falling-film evaporator is connected with a raw steam pipe, and a first-effect evaporator condensate water outlet at the lower part of the shell pass of the first-effect falling-film evaporator is connected with an inlet of a condensate water tank through a first-effect condensate water pipe; the material separation port at the lower part of the first-effect falling-film evaporator is connected with a first-effect separator through a communicating pipe, the steam exhaust port of the first-effect separator at the top part of the first-effect separator is connected with the steam exhaust pipe of the first-effect separator, the material liquid outlet of the first-effect separator at the bottom part of the first-effect separator is connected with the first-effect material liquid descending pipe, the lower end of the first-effect material liquid descending pipe is connected with the inlet of a first-effect circulating pump, the outlet of the first-effect circulating pump is connected with the circulating liquid inlet of the first-effect evaporator at the top part of the first-effect falling-film evaporator through a first-effect circulating pipe, and the outlet of the first-effect circulating pump is also connected with a material liquid output pipe;
the lower part of the two-effect falling-film evaporator is connected with a two-effect feed liquid descending pipe, the middle part of the two-effect feed liquid descending pipe is provided with a two-effect evaporator feed liquid inlet, the two-effect evaporator feed liquid inlet is connected with the outlet of the first-effect feed liquid output pipe, the outlet of the first-effect separator steam exhaust pipe is connected with a two-effect evaporator steam inlet at the upper part of the shell pass of the two-effect falling-film evaporator, and a two-effect evaporator condensate outlet at the lower part of the shell pass of the two-effect falling-film evaporator is connected with a two-effect condensate pipe; the material separation port at the lower part of the dual-effect falling-film evaporator is connected with a dual-effect separator through a communicating pipe, the steam exhaust port of the dual-effect separator at the top of the dual-effect separator is connected with the steam exhaust pipe of the dual-effect separator, the feed liquid outlet of the dual-effect separator at the bottom of the dual-effect separator is connected with the dual-effect feed liquid descending pipe, the lower end of the dual-effect feed liquid descending pipe is connected with the inlet of a dual-effect circulating pump, the outlet of the dual-effect circulating pump is connected with the circulating liquid inlet of the dual-effect evaporator at the top of the dual-effect falling-film evaporator through a dual-effect circulating pipe, and the outlet of the dual-effect circulating pump is also connected with a dual-effect feed liquid output pipe;
the top of the triple-effect crystallizer is provided with a triple-effect crystallizer exhaust port, the middle part of the circumferential wall of the triple-effect crystallizer is provided with a triple-effect crystallizer feed inlet, a triple-effect crystallizer circulation port and a triple-effect crystallizer return port, the bottom of the triple-effect crystallizer is provided with a triple-effect crystallizer discharge port, and the triple-effect crystallizer feed inlet is connected with the outlet of the double-effect feed liquid output pipe; a triple-effect auxiliary heater is connected below the discharge port of the triple-effect crystallizer, the discharge port at the lower end of the triple-effect auxiliary heater is connected with the inlet of a triple-effect circulating pump through a triple-effect descending circulating pipe, the outlet of the triple-effect circulating pump is connected with the feed port at the lower end of the triple-effect heater through a triple-effect ascending circulating pipe, the discharge port at the upper end of the triple-effect heater is connected with the circulating port of the triple-effect crystallizer, and the outlet of the triple-effect circulating pump is also connected with a triple-effect crystal slurry output pipe; the exhaust port of the triple-effect crystallizer is connected with the exhaust pipe of the triple-effect crystallizer; the outlet of the steam exhaust pipe of the two-effect separator is connected with the steam inlet of the three-effect heater on the upper part of the shell pass of the three-effect heater, the outlet of the two-effect condensate pipe is connected with the three-effect condensate inlet on the lower part of the shell pass of the three-effect heater, and the three-effect condensate outlet on the lower part of the shell pass of the three-effect heater is connected with the three-effect condensate pipe; the outlet of the steam exhaust pipe of the two-effect separator is also connected with the steam inlet of the three-effect auxiliary heater on the upper part of the shell pass of the three-effect auxiliary heater, the outlet of the two-effect condensate pipe is also connected with the three-effect auxiliary condensate inlet on the lower part of the shell pass of the three-effect auxiliary heater, and the three-effect auxiliary condensate outlet on the lower part of the shell pass of the three-effect auxiliary heater is connected with the three-effect auxiliary condensate pipe.
2. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 1, characterized in that: still include the one-level pre-heater, the bottom export of condensate water pitcher links to each other with condensate pump's entry, condensate pump's export pass through the comdenstion water delivery pipe with the one-level pre-heater water inlet of one-level pre-heater links to each other, the one-level pre-heater delivery port of one-level pre-heater links to each other with the comdenstion water recovery pipe, the one-level pre-heater feed liquid entry of one-level pre-heater with the export of charge pump links to each other, the one-level pre-heater feed liquid export of one-level pre-heater with a single-effect evaporator feed liquid entry links to each other.
3. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 2, characterized in that: the feed liquid outlet of the primary preheater is connected with the feed liquid inlet of the secondary preheater, and the feed liquid outlet of the secondary preheater is connected with the feed liquid inlet of the primary evaporator; and a secondary preheater steam inlet of the secondary preheater is connected with the steam generation pipe, and a secondary preheater condensate water outlet of the secondary preheater is connected with a water inlet of the condensate water tank through a high-temperature condensate water return pipe.
4. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 1, characterized in that: the lower end of the triple-effect downward circulating pipe is also connected with an inlet of a triple-effect crystal slurry pump, an outlet of the triple-effect crystal slurry pump is connected with a feed inlet of a triple-effect swirler, a top outlet of the triple-effect swirler is connected with a reflux port of the triple-effect crystallizer through a triple-effect crystal slurry reflux pipe, a bottom outlet of the triple-effect swirler is connected with an inlet of a thick tank, a bottom outlet of the thick tank is connected with an upper feed inlet of a centrifugal machine, and a solid phase outlet of the centrifugal machine is connected with a salt collecting system; and a liquid phase outlet of the centrifuge and an overflow port of the thick tank at the upper part of the thick tank are respectively connected with an inlet of the mother liquid tank.
5. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 4, characterized in that: the four-effect crystallizer is characterized by further comprising a four-effect crystallizer, wherein a four-effect crystallizer steam exhaust port is formed in the top of the four-effect crystallizer, a four-effect crystallizer circulation port and a four-effect crystallizer reflux port are formed in the middle of the circumferential wall of the four-effect crystallizer, and a four-effect crystallizer discharge port is formed in the bottom of the four-effect crystallizer; a four-effect auxiliary heater is connected below the discharge port of the four-effect crystallizer, the discharge port at the lower end of the four-effect auxiliary heater is connected with the inlet of a four-effect circulating pump through a four-effect descending circulating pipe, the outlet of the four-effect circulating pump is connected with the feed port at the lower end of the four-effect heater through a four-effect ascending circulating pipe, and the discharge port at the upper end of the four-effect heater is connected with the circulating port of the four-effect crystallizer; the outlet of the triple-effect crystal slurry output pipe is connected with the four-effect downward circulating pipe, and the exhaust port of the four-effect crystallizer is connected with the exhaust pipe of the four-effect crystallizer; the outlet of the three-effect crystallizer steam exhaust pipe is connected with the shell side steam inlet of the four-effect heater on the upper part of the shell side of the four-effect heater, the outlet of the three-effect condensate pipe is connected with the condensate inlet of the four-effect heater on the lower end of the four-effect heater, and the condensate outlet of the four-effect heater on the lower part of the shell side of the four-effect heater is connected with the condensate pipe of the four-effect heater; the outlet of the three-effect crystallizer exhaust pipe is also connected with the inlet of a four-effect auxiliary heater on the upper part of the shell side of the four-effect auxiliary heater, the outlet of the three-effect auxiliary condensate pipe is connected with the condensate inlet of the four-effect auxiliary heater on the lower end of the four-effect auxiliary heater, and the condensate outlet of the four-effect auxiliary heater on the lower part of the shell side of the four-effect auxiliary heater is connected with the four-effect condensate pipe; the outlet of the four-effect condensate pipe is connected to the inlet of the solvent tank, the bottom of the solvent tank is connected with the inlet of the solvent pump, and the outlet of the solvent pump is connected with the solvent output pipe.
6. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 5, characterized in that: the lower end of the four-effect downward circulating pipe is also connected with an inlet of a four-effect crystal slurry pump, an outlet of the four-effect crystal slurry pump is connected with a feed inlet of a four-effect swirler, a top outlet of the four-effect swirler is connected with a reflux port of the four-effect crystallizer through a four-effect crystal slurry reflux pipe, and a bottom outlet of the four-effect swirler is connected with an inlet of the thick tank; the outlet of the mother liquor tank is connected with the inlet of a mother liquor pump, and the outlet of the mother liquor pump is connected with a mother liquor filling port of the four-effect crystallizer in the middle of the circumferential wall of the four-effect crystallizer through a mother liquor return pipe.
7. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 6, characterized in that: an outlet of the four-effect crystallizer steam exhaust pipe is connected with an air inlet at the upper end of a shell pass of the surface condenser, and a condensate liquid exhaust port at the lower end of the shell pass of the surface condenser is connected with an inlet of the solvent tank through a surface condenser return pipe; the exhaust port at the lower end of the shell pass of the surface condenser is connected with a suction port of a water-ring vacuum pump, the exhaust port of the water-ring vacuum pump is connected with an exhaust pipe of the vacuum pump, a machine-sealed water outlet of the water-ring vacuum pump is connected with a circulating water tank of the vacuum pump, the bottom of the circulating water tank of the vacuum pump is connected with an inlet of a circulating water pump, and an outlet of the circulating water pump is connected with a machine-sealed water inlet of the water-ring vacuum pump.
8. The sodium chloride methanol aqueous solution evaporation recovery system according to claim 7, characterized in that: the top parts of the stock solution storage tank and the solvent tank and the upper and lower parts of the shell pass of the two-effect falling film evaporator, the three-effect heater, the three-effect auxiliary heater, the four-effect heater and the four-effect auxiliary heater are respectively provided with a non-condensable gas exhaust port, each non-condensable gas exhaust port is respectively connected with a non-condensable gas exhaust main pipe, and the outlet of the non-condensable gas exhaust main pipe is connected with the gas inlet at the upper end of the surface condenser; the top of the condensate water tank is connected with a condensate water tank steam exhaust pipe, and the outlet of the condensate water tank steam exhaust pipe and the exhaust port on the upper part and the lower part of the shell pass of the one-effect falling film evaporator are respectively connected with the steam inlet of the two-effect evaporator or the non-condensable gas exhaust main pipe.
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