CN217246844U

CN217246844U - Steam evaporation device with online recovery function

Info

Publication number: CN217246844U
Application number: CN202220195544.8U
Authority: CN
Inventors: 丁仁建
Original assignee: Yangzhou Ruibang Chemical Industry Technique
Current assignee: Yangzhou Ruibang Technology Development Co ltd
Priority date: 2022-01-24
Filing date: 2022-01-24
Publication date: 2022-08-23
Anticipated expiration: 2032-01-24

Abstract

The utility model relates to the technical field of new material production equipment, in particular to a steam evaporation device with on-line recovery, which comprises a heat exchanger, a rectifying tower, a condenser, a reflux tank, a low-boiling-point substance receiving tank and an ethylene glycol evaporator; the heat exchanger is communicated with the middle part of the rectifying tower, the upper part of the rectifying tower is communicated with one end of the condenser, the other end of the condenser is respectively communicated with the rectifying tower and the low-boiling-point substance receiving tank through the reflux tank, and the bottom of the rectifying tower is communicated with the ethylene glycol evaporator. The ethylene glycol purified by the device of the utility model can be directly fed into the evaporator for use without cooling and storage, the heat supply load of the evaporator is greatly reduced, and the total energy consumption is increased little; because the on-line continuous recovery and purification is adopted, the treatment capacity is small, the equipment investment is low, and a purified ethylene glycol storage tank is not needed; the full-automatic control saves labor cost.

Description

Steam evaporation device with online recovery function

Technical Field

The utility model relates to a new material production facility's technical field, concretely relates to take steam evaporation plant of online recovery.

Background

The vacuum system is an important component of a polyester production device, in the polycondensation stage of the polyester production process, the polycondensation reaction releases a lot of low molecular weight Ethylene Glycol (EG) and compounds thereof while producing high molecular weight polymers, and in order to ensure that the polycondensation reaction is smoothly carried out and obtain polyester products with excellent quality, small molecular substances generated by the reaction must be rapidly separated out of the reaction system, so the polycondensation reaction is usually carried out under the reduced pressure of 100-1000 Pa (absolute).

At present, the vacuum generating device of most polyester production devices mainly adopts an ethylene glycol steam jet pump, in the using process, the purity of ethylene glycol steam has higher requirements, for example, the content of low boiling point components in the steam is higher, partial pressure can be generated in a vacuum state, the air suction quantity of a vacuum pump is influenced, the limit pressure in a polycondensation system is increased, the reaction speed is influenced, in the using process, low boiling point substances and a small part of low boiling point substances such as water, acetaldehyde and the like extracted from a reaction kettle are decomposed and produced under the high temperature of ethylene glycol, the performance of the vacuum pump is inevitably influenced, the normal use can be ensured only by continuously replacing the low boiling point substances with pure ethylene glycol, the replaced ethylene glycol can be used only by purifying through an independent purifying device, the energy consumption is increased, or a working section with low requirements on the purity of ethylene glycol is used. How to recycle the sprayed glycol without pure glycol replacement is a problem to be solved.

SUMMERY OF THE UTILITY MODEL

In order to solve the technical problem in this application, the utility model provides a take steam evaporation device of online recovery.

The utility model provides a following technical scheme: a vapor evaporation device with on-line recovery comprises a heat exchanger, a rectifying tower, a condenser, a reflux tank, a low-boiling-point substance receiving tank and an ethylene glycol evaporator; the heat exchanger is communicated with the middle part of the rectifying tower, the upper part of the rectifying tower is communicated with one end of the condenser, the other end of the condenser is respectively communicated with the rectifying tower and the low-boiling-point substance receiving tank through the reflux tank, and the bottom of the rectifying tower is communicated with the ethylene glycol evaporator.

Further, heating coil, liquid level transmitter and temperature transmitter one are installed to the bottom of rectifying column, the top of rectifying column is equipped with temperature transmitter two.

Furthermore, an emptying pipe is installed on the reflux tank.

Furthermore, an evaporation heating pipe is arranged in the ethylene glycol evaporator, and an evaporator feed adjusting valve is arranged on a pipeline between the ethylene glycol evaporator and the rectifying tower.

Further, the ethylene glycol evaporator is communicated with the heat exchanger through a steam jet pump.

The utility model relates to a take steam evaporation plant of online recovery, its beneficial effect: 1. the purified glycol is directly fed into an evaporator for use without being cooled and stored, the heat supply load of the evaporator is greatly reduced, and the total energy consumption is increased little; 2. because the on-line continuous recovery and purification is adopted, the treatment capacity is small, the equipment investment is low, and a purified ethylene glycol storage tank is not needed; 3. the full-automatic control saves labor cost; 4. the PET waste recycling device is particularly suitable because the PET waste recycling device does not consume ethylene glycol and replaced ethylene glycol cannot be consumed.

Drawings

The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention, and together with the description serve to explain the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic diagram of the device of the present invention;

labeled as: 1. a heat exchanger; 2. a rectifying tower; 3. a condenser; 4. a reflux tank; 5. a low-boiling-point substance receiving tank; 6. a glycol evaporator; 7. a glycol feed regulating valve; 8. an emptying pipe; 9. an evaporator heating tube; 10. a heating coil; 11. an evaporator feed regulating valve; 12. a heat conducting oil regulating valve of the heat exchanger; 13. a reflux regulating valve; 14. an evaporator pressure regulating valve.

Detailed Description

The conception, specific structure and technical effects of the present invention will be described clearly and completely with reference to the accompanying drawings and embodiments, so as to fully understand the objects, aspects and effects of the present invention. It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict. It should be noted that, unless otherwise specified, when a feature is referred to as being "fixed" or "connected" to another feature, it can be directly fixed or connected to the other feature or indirectly fixed or connected to the other feature. Furthermore, the description of the upper, lower, left, right, etc. used in the present invention is only relative to the mutual positional relationship of the components of the present invention in the drawings.

As shown in fig. 1, a vapor evaporation device with on-line recovery comprises a heat exchanger 1, a rectifying tower 2, a condenser 3, a reflux tank 4, a low-boiling-point substance receiving tank 5 and an ethylene glycol evaporator 6; the heat exchanger 1 is communicated with the middle of the rectifying tower 2 and used for improving the feeding temperature of ethylene glycol, an ethylene glycol feeding adjusting valve 7 is arranged on a feeding pipeline and used for controlling the liquid level at the bottom of the rectifying tower 2, the heat exchanger 1 is heated by heat conduction oil or steam, a heating medium is automatically controlled by the ethylene glycol temperature adjusting valve, the temperature of the ethylene glycol at the outlet of the heat exchanger 1 is controlled at 140-220 ℃, the upper part of the rectifying tower 2 is communicated with one end of the condenser 3, the other end of the condenser 3 is communicated with the rectifying tower 2 and the low-boiling-point substance receiving tank 5 respectively through the reflux tank 4, and the bottom of the rectifying tower 2 is communicated with the ethylene glycol evaporator 6. The rectifying tower 2 is a packed tower, and is internally provided with corrugated wire mesh packing, so that a sufficient contact surface is provided for gas and liquid phases, and conditions are created for improving the turbulence degree (mainly gas phase) of the tower, thereby being beneficial to mass transfer and heat transfer. The bottom of tower is equipped with heating coil 10, gives the material heating through the outside heat source, provides the heat that the rectification needs, and the bottom of tower is equipped with liquid level transmitter, temperature transmitter one in addition, and ethylene glycol feed governing valve 7 and the liquid level chain control at the bottom of the tower, and the top of tower is equipped with temperature transmitter two, and the control of top of the tower temperature is at 100 ~ 140 ℃.

The receiving line sets up in 4 sides of backward flow jar, and the backward flow pipeline sets up in 4 bottoms of backward flow jar, and the preferential back flow line flow that satisfies, under the normal condition, 4 liquid levels of backward flow jar are in receiving tube department, and when the top of the tower temperature is high, when needing the increase reflux volume, the liquid of 4 internal storages of backward flow jar can satisfy the requirement. And the return tank 4 is provided with an emptying pipe 8 for discharging non-condensable gas, so that the system is kept in a normal pressure state.

Refined ethylene glycol enters an ethylene glycol evaporator 6 through a pipeline at the bottom of the rectifying tower 2, an evaporator heating pipe 9 is arranged in the evaporator, and materials are heated through an external heat source to provide heat required by ethylene glycol evaporation. An external heat source is interlocked with a pressure transmitter through an evaporator pressure regulating valve to control the pressure in the evaporator to be 10 KPA-150 KPA, an evaporator feeding regulating valve 11 is arranged on a pipeline between the bottom of a rectifying tower 2 and an ethylene glycol evaporator 6, the liquid level is controlled to be 30% -60% through interlocking with a liquid level transmitter, and steam generated by the evaporator is conveyed to an ethylene glycol steam jet pump through a steam pipeline for use.

The utility model discloses install theory of operation:

the ethylene glycol used by the steam jet pump and with the content of the low boiling point components exceeding the standard is heated by a heat exchanger and then sent to a rectifying tower to remove the low boiling point components, and the ethylene glycol at the bottom of the tower enters an evaporator to be heated to generate steam for the jet pump to use. The liquid level at the bottom of 2 towers of rectifying column passes through ethylene glycol feed control valve 7 control, and the temperature at the bottom of 2 towers of rectifying column passes through heat exchanger conduction oil governing valve 12 control, and 2 top temperature of rectifying column pass through backflow regulating valve 13 control, and evaporimeter pressure passes through evaporimeter pressure regulating valve 14 control, and the evaporimeter liquid level passes through evaporimeter feed control valve 11 control, and whole process is full-automatic, need not manual operation.

Although the present invention has been described in detail with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described in the foregoing embodiments, or equivalents may be substituted for elements thereof. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims

1. A steam evaporation device with on-line recovery is characterized by comprising a heat exchanger, a rectifying tower, a condenser, a reflux tank, a low-boiling-point substance receiving tank and an ethylene glycol evaporator; the heat exchanger communicate in the rectifying column middle part, the upper portion of rectifying column communicate in the one end of condenser, the other end of condenser passes through the reflux drum communicate respectively in the rectifying column with low boiling thing holding vessel, the bottom of rectifying column communicate in the ethylene glycol evaporimeter.

2. The steam evaporation device with the on-line recovery function as claimed in claim 1, wherein a heating coil, a liquid level transmitter and a first temperature transmitter are mounted at the bottom of the rectifying tower, and a second temperature transmitter is mounted at the top of the rectifying tower.

3. The vapor-evaporating apparatus with on-line recovery of claim 2, wherein the reflux drum is fitted with a blow-down pipe.

4. The vapor evaporation device with on-line recovery as recited in claim 3, wherein an evaporation heating pipe is disposed inside the glycol evaporator, and an evaporator feed adjusting valve is disposed on a pipe between the glycol evaporator and the rectifying tower.

5. The vapor evaporation device with on-line recovery of claim 3, wherein the glycol evaporator is in communication with the heat exchanger through a vapor jet pump.