CN217988400U - Recovery unit of well low concentration ethylene glycol aqueous solution - Google Patents
Recovery unit of well low concentration ethylene glycol aqueous solution Download PDFInfo
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- CN217988400U CN217988400U CN202222120030.9U CN202222120030U CN217988400U CN 217988400 U CN217988400 U CN 217988400U CN 202222120030 U CN202222120030 U CN 202222120030U CN 217988400 U CN217988400 U CN 217988400U
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Abstract
The utility model relates to a technical field is retrieved to the coolant liquid, discloses a recovery unit of well low concentration ethylene glycol aqueous solution, and the device includes: the device comprises a feeding unit, a preheating unit, an evaporation concentration unit, a steam compression unit, a discharging unit and a vacuum unit which are connected through pipelines, wherein the preheating unit is used for preheating ethylene glycol aqueous solution provided by the feeding unit, the evaporation concentration unit is used for evaporating and concentrating the ethylene glycol aqueous solution preheated by the preheating unit, the steam compression unit is used for compressing secondary steam generated in the evaporation concentration unit, and the discharging unit is used for discharging the recovered ethylene glycol aqueous solution; the feeding of the feeding unit is an aqueous solution with the concentration of ethylene glycol of 5% -40%, and the discharging of the discharging unit is an aqueous solution with the concentration of ethylene glycol of more than 60%. The utility model discloses the convenience is retrieved the low-middle concentration ethylene glycol aqueous solution that feed concentration changes.
Description
Technical Field
The utility model relates to a technical field is retrieved to the coolant liquid, especially relates to a recovery unit of well low concentration ethylene glycol aqueous solution.
Background
In recent years, antifreeze, refrigerating fluid and deicing fluid are ethylene glycol aqueous solutions which are most commonly applied to the industry and aviation industry, with the rapid development of the industry and aviation industry, the demand of the ethylene glycol solution is increasing day by day, in the long-term circulation process of the antifreeze and the refrigerating fluid, due to the low temperature, the concentration of the antifreeze and the refrigerating fluid is reduced due to the absorption of partial moisture in the air, and meanwhile, the concentration of the ethylene glycol solution serving as the deicing fluid is reduced due to the absorption of moisture after ice melting.
At present, the ethylene glycol source in China mainly depends on chemical production, and the synthesis process comprises various synthesis methods including preparation of ethylene glycol from coal and preparation of ethylene glycol from synthesis gas;
for the petrochemical field, a process for preparing ethylene glycol from ethylene is commonly used, ethylene is added with chlorine to prepare dichloroethane, and the dichloroethane is hydrolyzed under an alkaline condition to generate ethylene glycol, wherein under an ideal condition, the process needs to consume equivalent ethylene, and in order to improve the conversion rate of ethylene addition, a large amount of chlorine serving as another raw material needs to be input;
the synthetic process not only consumes more water, and the accessory substance treatment that produces in addition the in-process also is one of the difficult problems that need solve, consequently, the utility model provides a recovery unit of well low concentration ethylene glycol aqueous solution provides the technical route that a well low concentration ethylene glycol aqueous solution was retrieved.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model lies in how to provide a recovery unit of well low concentration ethylene glycol aqueous solution to it retrieves well low concentration ethylene glycol aqueous solution to make things convenient for.
Therefore, according to the first aspect, the embodiment of the utility model discloses a recovery unit of well low concentration ethylene glycol aqueous solution, include: the system comprises a feeding unit, a preheating unit, an evaporation concentration unit, a steam compression unit, a discharging unit and a vacuum unit which are connected through pipelines, wherein the preheating unit is used for preheating a glycol aqueous solution provided by the feeding unit, the evaporation concentration unit is used for carrying out evaporation concentration on the glycol aqueous solution preheated by the preheating unit, the steam compression unit is used for compressing secondary steam escaping from the evaporation concentration unit, and the discharging unit is used for discharging the recovered glycol aqueous solution; the feeding of the feeding unit is an aqueous solution with the concentration of ethylene glycol of 5% -40%, and the discharging of the discharging unit is an aqueous solution with the concentration of ethylene glycol of more than 60%.
The utility model discloses further set up to, the feed unit includes mutual tube coupling's head tank and head pump, the head pump be used for with ethylene glycol aqueous solution in the head tank is taken out extremely preheat the unit.
The utility model discloses further set up to, the head pump is wide flow inverter pump.
The utility model discloses further set up to, preheat the arbitrary one or more in unit for concentrate preheater, secondary steam comdenstion water preheater and the raw steam preheater.
The utility model discloses further set up to, the evaporation concentration unit includes falling film evaporator, filler knockout tower, falling film circulating pump, backwash pump and condensate tank, falling film evaporator's upper end with the export tube coupling of falling film circulating pump, falling film evaporator's lower ware body with filler knockout tower tube coupling, falling film evaporator's lower extreme with filler knockout tower's lower extreme with the entry tube coupling of falling film circulating pump, falling film evaporator condensate tank the backwash pump with filler knockout tower tube coupling in proper order.
The utility model discloses further set up to, falling film evaporator is vertical falling film heat exchanger or violently manages falling film heat exchanger.
The utility model discloses further set up to, the packing layer top of filler knockout tower is equipped with the feed liquid distributor, the top of feed liquid distributor is equipped with the demister.
The utility model discloses further set up to, the vapor compression unit includes compressor unit and compressor spray water pump, the compressor unit with the evaporation concentration unit tube coupling, the export of compressor spray water pump with the spiral case tube coupling of compressor unit, the import and outside deionized water or soft water source tube coupling of compressor spray water pump.
The utility model discloses further set up to, the vapor compression unit still includes compressor hydrops jar and compressor hydrops pump, the compressor unit the compressor hydrops jar and the compressor hydrops pump tube coupling in proper order.
The utility model discloses further set up to, ejection of compact unit includes distilled water pump and discharge pump, distilled water pump with the discharge pump respectively with evaporation concentration unit tube coupling.
The utility model discloses further set up to, ejection of compact unit still includes congeals water cooler and ejection of compact cooler, congeal the water cooler with ejection of compact cooler respectively with preheat unit tube coupling.
The utility model discloses further set up as, the vacuum unit includes mutual pipe connection's not condensed condenser cooler and vacuum pump, not condensed condenser cooler with evaporation concentration unit tube coupling.
The utility model discloses following beneficial effect has: it is right through preheating the unit the ethylene glycol aqueous solution that the feed unit provided preheats, and the evaporation concentration unit carries out evaporation concentration to the ethylene glycol aqueous solution after preheating the unit and preheating, and the secondary steam that produces in the evaporation concentration unit is compressed to the vapor compression unit, and ejection of compact unit is used for discharging the ethylene glycol aqueous solution after retrieving, and then provides the recovery unit of well low concentration ethylene glycol aqueous solution, conveniently retrieves well low concentration ethylene glycol aqueous solution.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.
FIG. 1 is a schematic structural diagram of a recovery apparatus for a medium/low concentration ethylene glycol aqueous solution disclosed in this embodiment;
FIG. 2 is a schematic flow chart of a method for recovering a middle-low concentration ethylene glycol aqueous solution disclosed in this embodiment.
Reference numerals are as follows: 1. a stock tank; 2. a feedstock pump; 3. a concentrated material preheater; 4. a secondary steam condensate water preheater; 5. a raw steam preheater; 6. a falling film evaporator; 7. a packed separation column; 8. a falling film circulating pump; 9. a reflux pump; 10. a condensate tank; 11. a compressor unit; 12. a compressor liquid accumulation tank; 13. a compressor liquid accumulation pump; 14. a compressor spray water pump; 15. a distilled water pump; 16. a discharge pump; 17. a non-condensing condenser cooler; 18. and a vacuum pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected" and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; the two elements may be directly connected or indirectly connected through an intermediate medium, or may be communicated with each other inside the two elements, or may be wirelessly connected or wired connected. The specific meaning of the above terms in the present invention can be understood as a specific case by those skilled in the art.
In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", and the like indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplification of description, but do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
Furthermore, the technical features mentioned in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.
The recovery device for a middle-low concentration ethylene glycol aqueous solution disclosed in this embodiment, as shown in fig. 1, includes a feeding unit, a preheating unit, an evaporation and concentration unit, a vapor compression unit, a discharging unit, a vacuum system, and an automatic control system responsible for detecting and controlling operation parameters, which are connected by a pipeline; the feeding unit comprises a raw material tank 1 and a raw material pump 2 which are connected in sequence; a raw material tank 1 is arranged at the inlet side of the raw material pump 2, and the outlet side of the raw material pump 2 is connected with a concentrated material preheater;
the preheating unit comprises a concentrated material preheater 3, a secondary steam condensate water preheater 4 and a raw steam preheater 5 which are sequentially connected through pipelines;
the evaporation concentration unit comprises a falling film evaporator 6, a filler separation tower 7, a falling film circulating pump 8, a reflux pump 9 and a condensate tank 10 which are sequentially connected through pipelines;
the vapor compression unit comprises a compressor unit 11, a compressor liquid accumulation tank 12, a compressor liquid accumulation pump 13 and a compressor spray water pump 14 which are sequentially connected through pipelines;
the discharging unit comprises a distilled water pump 15 and a discharging pump 16;
the vacuum system comprises a non-condensing condenser cooler 17 and a vacuum pump 18 which are connected in sequence; an inlet of the vacuum pump 18 is connected with a hot side outlet of the non-condensing cooler 17, and a cold side inlet of the non-condensing cooler 17 is connected with a hot side of the falling film evaporator 6.
The glycol water solution provided by the feeding unit is preheated by the preheating unit, the glycol water solution preheated by the preheating unit is evaporated and concentrated by the evaporation and concentration unit, secondary steam escaping from the evaporation and concentration unit is compressed by the steam compression unit, and the discharge unit is used for discharging the recovered glycol water solution, so that the recovery device for the glycol water solution with medium and low concentration is provided, and the recovery device for the glycol water solution with medium and low concentration is convenient to recover the glycol water solution with medium and low concentration.
As shown in fig. 1, one side of the secondary steam condensate water preheater 4 is provided with a concentrate preheater 3, the other side of the secondary steam condensate water preheater 4 is provided with a raw steam preheater 5, the secondary steam condensate water preheater 4 and the raw steam preheater 5 are connected with an inlet and an outlet through cold testing each other, the inlet of the hot side of the concentrate preheater 3 is connected with the outlet of the discharge pump 16, the inlet of the hot side of the secondary steam condensate water preheater 4 is connected with the outlet of the distilled water pump 15, the inlet of the hot side of the raw steam preheater 5 is connected with a steam supply pipe of public engineering, and the outlet of the hot side of the raw steam preheater 5 is connected with the condensate tank 10.
As shown in fig. 1, the upper end of the falling film evaporator 6 is connected with an outlet of a falling film circulating pump 8, the lower body of the falling film evaporator 6 is connected with a filler separating tower 7, the lower end of the filler separating tower 7 is connected with an inlet of the falling film circulating pump 8 to form a loop, the loop is provided with a cold side outlet connected with a raw steam preheater 5, the filler separating tower 7 is arranged behind the falling film evaporator 6, the upper part of the filler separating tower 7 is connected with an inlet of a compressor unit 11, the filler separating tower 7 is provided with a liquid distributor, an inlet of the liquid distributor is connected with an outlet of a reflux pump 9, and an inlet of the reflux pump 9 is connected with a condensate tank 10.
As shown in fig. 1, the falling film evaporator 6 is a vertical falling film heat exchanger or a horizontal tube falling film heat exchanger; if the falling film evaporator 6 is a vertical falling film heat exchanger, the shell pass of the heat exchanger is a hot side, and the tube pass is cold testing; if the falling film evaporator 6 is a horizontal tube falling film heat exchanger, the shell pass of the heat exchanger is a cold side, and the tube pass is a hot side.
As shown in fig. 1, an outlet of a compressor spray water pump 14 is connected with a volute of a compressor unit 11, a compressor liquid accumulation tank 12 is positioned below the compressor unit 11, one side of the compressor liquid accumulation tank 12 is connected with a compressor liquid accumulation pump 13, an inlet of the compressor unit 11 is connected with a packing separation tower 7, and an outlet of the compressor unit 11 is connected with a hot side of a falling film evaporator 6.
As shown in fig. 1, an inlet of a distilled water pump 15 is connected with a condensate tank 10, an outlet of the distilled water pump 15 is connected with a secondary steam condensate water preheater 4, an inlet of a discharge pump 16 is connected with the lower part of a falling film evaporator 6, and an outlet of the discharge pump 16 is connected with a concentrate preheater 3.
In the specific implementation process, the automatic control system is a PLC control system; further, the automatic control system selects a DCS distributed control system.
In the specific implementation process, the treatment device of the glycol solution is suitable for treating the aqueous solution with the temperature of more than 25 ℃ and the glycol mass fraction of 15-40%, the evaporation capacity of the treatment device is about 2000kg/h, and the design pressure of the device is 0.6bar. The compressor unit 11 of the vapor compression unit can raise the temperature of the vapor by more than or equal to 15 ℃, and can provide the operational flexibility of 120% of the maximum flow.
In the specific implementation process, the reflux pump 9 and the distilled water pump 15 are both variable frequency pumps, the operation flow rates of the variable frequency pumps can be adjusted in a variable frequency mode, the actual flow rate ratio is a reflux ratio, the designed reflux ratio is 0.1, the actual operation is adjusted to be 0.08-0.2 through the variable frequency adjustment, the reflux ratio can be adjusted to change the content of the secondary steam condensed water glycol, and the value of the reflux ratio can be adjusted through an automatic control system.
In the specific implementation process, a material liquid distributor is arranged above a packing layer of the packing separation tower 7, and a demister is arranged above the material liquid distributor, so that the air flow can be prevented from carrying liquid drops to enter the compressor, and the impeller of the compressor is protected. 15. The theoretical plate number of the packing layer of the packing separation tower 7 is more than 3, and the height of the packing layer is more than 0.6 m.
In the specific implementation process, the automatic control system is provided with an Abbe refractometer, and can measure the concentration of ethylene glycol in feed liquid of a lower device body of the feeding and falling-film evaporator 6 so as to analyze and control relevant operating conditions.
As shown in fig. 1 and fig. 2, the working process is as follows, the raw material of the raw material tank 1 enters a concentrated material preheater 3, a secondary steam condensate preheater 4 and a raw steam preheater 5 through a raw material pump 2 for preheating, the preheated raw material enters a falling film evaporator 6 after reaching the bubble point temperature of the raw material liquid under the operating pressure, the ethylene glycol aqueous solution is circulated in the falling film evaporator and continuously subjected to heat exchange evaporation with the hot side under the circulating drive of a falling film circulating pump 8, the evaporation temperature of the falling film evaporator 6 is 96.5 ℃, the pressure is 58kPa, the generated secondary steam is escaped to a filler separation tower 7 through a connecting pipeline and then enters a compressor unit 11, the temperature of the secondary steam after temperature rise and pressure rise is about 106 ℃, the pressure is 125kPa, the secondary steam returns to the falling film evaporator 6 again to be used as a heating source, and is liquefied into secondary steam condensate after heat utilization and flows into a condensate tank 10; the secondary steam condensate in the condensate tank can be pumped out by a reflux pump and is pumped into the inlet of a liquid distributor of a packing separation tower 7, the feed liquid dispersed by the liquid distributor is in gas-liquid contact with the rising steam in the filler separation tower for gas-liquid contact, and the glycol in the gas phase is absorbed by the feed liquid, so that the purpose of rectification is achieved, and the glycol concentration of the discharged secondary steam condensate is reduced;
when the concentration of glycol in the feed liquid of the lower device body of the falling-film evaporator 6 reaches more than 60%, the feed liquid is pumped out by the discharge pump 16 and pumped into the concentrated material preheater 3 to exchange heat with a newly-fed raw material, so that the heat recovery process is completed;
the feed liquid contains a small amount of dissolved air or a device has a small amount of air leakage, non-condensed steam can be formed in the evaporation process, and the feed liquid is primarily cooled by a vacuum pump 18 for adjusting the vacuum degree of the system through a non-condensed steam cooler 17 with circulating cooling water and then is pumped out of a system boundary area;
in the specific implementation process, when the ethylene glycol solution with the feed ethylene glycol concentration of 5% is processed, the condensation amount of secondary steam at the hot side of the falling-film evaporator 6 is about 2160kg/h, under the condition that the reflux ratio is 0.08, about 2000kg/h of secondary steam condensate water is pumped out of the condensate tank 10 by the distilled water pump 15 and is pumped into the secondary steam condensate water preheater 4, and after heat recovery is carried out by heat exchange with raw materials, the secondary steam condensate water is discharged out of a system boundary area, and about 160kg/h of secondary steam condensate water is pumped into the inlet of the liquid distributor of the packing separation tower 7 by the reflux pump 9;
in the specific implementation process, when the ethylene glycol solution with the feed ethylene glycol concentration of 40% is treated, the condensation amount of the secondary steam at the hot side of the falling-film evaporator 6 is about 2300kg/h, under the condition that the reflux ratio is 0.15, about 2000kg/h of secondary steam condensate water is pumped out of the condensate tank 10 by the distilled water pump 15 and is pumped into the secondary steam condensate water preheater 4, the secondary steam condensate water is discharged out of a system boundary area after heat recovery is carried out on heat exchange with raw materials, and about 300kg/h of secondary steam condensate water is pumped into the inlet of the liquid distributor of the packing separation tower 7 by the reflux pump 9;
in the specific implementation process, the vacuum of different systems can be respectively controlled to a set value by interlocking the pressure of the systems through a vacuum pump, a pressure sensor and a regulating valve, so that the automatic control of the operating pressure is realized, and the automatic control of the feeding can be realized through a falling film evaporator 6 liquid level interlocking raw material pump 2 frequency converter; the automatic control of material transfer can be realized by monitoring the liquid phase temperature of the falling-film evaporator 6 and the gas phase temperature difference of the filler separation tower 7 on line; the whole automatic control system can realize high automation degree;
the automatic control system is provided with an Abbe refractometer for measuring the refractive index of an ethylene glycol-water system on line, and can conjecture the concentration of the fed ethylene glycol and automatically adjust the reflux quantity according to the refractive index caused by different ethylene glycol concentrations at the same temperature by combining a temperature sensor;
the condensate generated by the compressor unit 11 in the working process flows into the compressor condensate tank 12, the compressor condensate tank 12 is connected with the inlet of the compressor condensate pump 13, and the compressor condensate pump 13 pumps the condensate in the compressor condensate tank 12 into the condensate tank 10 to participate in system circulation; because the steam at the outlet of the compressor unit 11 is superheated steam and needs a certain amount of soft water for neutralization of superheat degree, the outlet of the compressor spray water pump 14 is connected with the desuperheating water connector of the compressor unit 11, and the inlet of the compressor spray water pump 14 is connected with the soft water supply outside the device;
in the embodiment, the vacuum of the system can be respectively controlled to a set value by interlocking different system pressures through a vacuum pump, a pressure sensor and a regulating valve, so that the automatic control of the operating pressure is realized, and the automatic control of the feeding can be realized through a liquid level interlocking feeding regulating valve of the falling film heat exchanger; the system can realize the automatic control of the feeding and discharging of the system through the regulating valve by monitoring the parameters such as temperature, flow, liquid level and refractive index on line, and the whole system can realize high automation degree.
The ethylene glycol aqueous solution treated by the method and the device for recovering the ethylene glycol aqueous solution with medium and low concentration disclosed by the embodiment has the ethylene glycol concentration of 5-40% and the operation parameters shown in the table 1.
TABLE 1 operating parameters
The method for recovering a middle-low concentration ethylene glycol aqueous solution disclosed in this embodiment, as shown in fig. 1 and fig. 2, includes the following steps:
s1, preheating raw materials, namely extracting a stock solution of a raw material tank 1 through a raw material pump 2, introducing the stock solution into a preheater, respectively flowing through a concentrate preheater 3, a secondary steam condensate preheater 4 and a raw steam preheater 5, respectively performing heat exchange preheating with a concentrate, secondary steam condensate and raw steam, preheating to a bubble point temperature under an operating pressure, and introducing into a falling film evaporator 6;
s2, evaporation and concentration, wherein after the material is introduced into the cold side of the falling film evaporator 6, the material is subjected to heat exchange evaporation with steam on the hot side of the falling film evaporator, part of the material is gasified, the purpose of concentrating the ethylene glycol solution is achieved, the rest unevaporated material liquid is remained in the lower device body of the falling film evaporator 6, is pumped out by a falling film circulating pump 8, is introduced into the top of the falling film evaporator 6, and participates in falling film evaporation circulation together with the preheated raw material; the compressed secondary steam on the hot side of the falling-film evaporator 6 is condensed into secondary steam condensate water after heat exchange with the cold-measured feed liquid, then the secondary steam condensate water flows into the condensate tank 10, and the reflux pump 9 is used for pumping out part of the secondary steam condensate water in the condensate tank 10 and introducing the condensate water into the filler separation tower 7;
s3, rectifying and absorbing, namely allowing the material steam gasified by the falling film evaporator 6 to escape to a packing separation tower 7 and generate gas-liquid contact conditions with secondary steam condensate, so that gas-liquid exchange is generated between the ascending gasified steam and the descending secondary steam condensate in an intermediate packing layer, and glycol of the material liquid steam is absorbed by the descending material liquid to reduce the concentration of the steam glycol;
s4, recompressing the steam, enabling secondary steam escaping from the upper part of the packing separation tower 7 to enter a compressor unit 11 through a process pipeline, heating and boosting the pressure after compression, enabling accumulated liquid generated in the process to flow into a compressor accumulated liquid tank 12 under the action of gravity, outputting compressed secondary steam under required conditions under the synergistic action of a compressor spray water pump 14 connected with soft water, and conveying the compressed secondary steam to the hot side of a falling film evaporator 6 of an evaporation concentration unit;
s5, heat recovery, wherein secondary steam condensate water in the condensate tank 10 is pumped out by a distilled water pump 15 and is introduced into a secondary steam condensate water preheater 4 of the preheating unit to exchange heat with the raw materials; the discharge pump 16 pumps out the concentrated feed liquid in the lower body of the falling-film evaporator 6, and the concentrated feed liquid is introduced into a concentrated feed preheater 3 of the preheating unit to exchange heat with the raw materials.
In the method and the device for recovering the ethylene glycol aqueous solution with the medium and low concentration disclosed by the embodiment, the energy-saving mechanical vapor recompression technology is adopted, and compared with the traditional rectification without adopting the mechanical vapor recompression technology, the process has high thermal efficiency and low power consumption, and about 1.5 tons of vapor can be saved by evaporating each ton of water; the ethylene glycol solution with a plurality of feeding concentrations can be dynamically treated, and the adaptability is strong; and the secondary steam compression is adopted as a circulating heat source, so that the dependence of a boiler can be reduced, the energy consumption is reduced, pollutants are reduced, the environmental pollution is reduced, and the energy-saving and environment-friendly effects are achieved. The device has the advantages of simple process flow, easy realization, high automation degree and low operation cost, meets the requirement of sustainable development, and can be widely applied to the actual industrial production process.
It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious changes and modifications can be made without departing from the scope of the invention.
Claims (12)
1. The utility model provides a recovery unit of well low concentration ethylene glycol aqueous solution which characterized in that includes: the system comprises a feeding unit, a preheating unit, an evaporation concentration unit, a steam compression unit, a discharging unit and a vacuum unit which are connected through pipelines, wherein the preheating unit is used for preheating a glycol aqueous solution provided by the feeding unit, the evaporation concentration unit is used for carrying out evaporation concentration on the glycol aqueous solution preheated by the preheating unit, the steam compression unit is used for compressing secondary steam escaping from the evaporation concentration unit, and the discharging unit is used for discharging the concentrated glycol aqueous solution;
the feeding of the feeding unit is an aqueous solution with the concentration of ethylene glycol of 5% -40%, and the discharging of the discharging unit is an aqueous solution with the concentration of ethylene glycol of more than 60%.
2. The apparatus for recovering ethylene glycol aqueous solution with medium and low concentration according to claim 1, wherein the feeding unit comprises a raw material tank and a raw material pump, wherein the raw material tank and the raw material pump are connected by a pipeline, and the raw material pump is used for pumping the ethylene glycol aqueous solution in the raw material tank to the preheating unit.
3. The apparatus for recovering ethylene glycol aqueous solution with medium/low concentration according to claim 2, wherein the raw material pump is a wide flow rate variable frequency pump.
4. The apparatus for recovering a middle/low concentration ethylene glycol aqueous solution according to claim 1, wherein the preheating unit is any one or more of a concentrate preheater, a secondary steam condensate preheater and a raw steam preheater.
5. The apparatus for recovering a middle/low-concentration ethylene glycol aqueous solution according to claim 1, wherein the evaporation concentration unit comprises a falling-film evaporator, a packing separation tower, a falling-film circulating pump, a reflux pump and a condensate tank, wherein the upper end of the falling-film evaporator is connected with an outlet pipeline of the falling-film circulating pump, the lower body of the falling-film evaporator is connected with a pipeline of the packing separation tower, the lower ends of the falling-film evaporator and the packing separation tower are connected with an inlet pipeline of the falling-film circulating pump, and the falling-film evaporator, the condensate tank, the reflux pump and the packing separation tower are sequentially connected with a pipeline.
6. The apparatus for recovering a middle/low concentration ethylene glycol aqueous solution according to claim 5, wherein the falling film evaporator is a vertical falling film heat exchanger or a horizontal tube falling film heat exchanger.
7. The apparatus for recovering ethylene glycol aqueous solution with medium and low concentration according to claim 5, wherein a feed liquid distributor is arranged above the packing layer of the packing separation tower, and a demister is arranged above the feed liquid distributor.
8. The apparatus for recovering ethylene glycol aqueous solution with medium or low concentration according to claim 1, wherein the vapor compression unit comprises a compressor unit and a compressor spray water pump, the compressor unit is connected with the evaporation concentration unit through a pipeline, an outlet of the compressor spray water pump is connected with a volute pipeline of the compressor unit, and an inlet of the compressor spray water pump is connected with an external deionized water or soft water source through a pipeline.
9. The apparatus for recovering ethylene glycol aqueous solution with medium and low concentration according to claim 8, wherein the vapor compression unit further comprises a compressor liquid accumulation tank and a compressor liquid accumulation pump, and the compressor unit, the compressor liquid accumulation tank and the compressor liquid accumulation pump are sequentially connected by a pipeline.
10. The apparatus for recovering a medium/low concentration ethylene glycol aqueous solution according to claim 1, wherein the discharge unit comprises a distilled water pump and a discharge pump, and the distilled water pump and the discharge pump are respectively connected to the evaporation and concentration unit through pipelines.
11. The apparatus for recovering ethylene glycol aqueous solution with medium and low concentration according to claim 10, wherein the discharging unit further comprises a condensate cooler and a discharging cooler, and the condensate cooler and the discharging cooler are respectively connected with the preheating unit through a pipeline.
12. The apparatus for recovering an aqueous solution of ethylene glycol having a medium/low concentration according to claim 1, wherein the vacuum unit comprises an uncondensed condenser and a vacuum pump connected to each other by a pipe, and the uncondensed condenser is connected to the evaporative concentration unit by a pipe.
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| CN202222120030.9U CN217988400U (en) | 2022-08-12 | 2022-08-12 | Recovery unit of well low concentration ethylene glycol aqueous solution |
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| CN202222120030.9U CN217988400U (en) | 2022-08-12 | 2022-08-12 | Recovery unit of well low concentration ethylene glycol aqueous solution |
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