F22 / HFP azeotrope extraction and separation device

Abstract

The utility model discloses an F22 / HFP azeotrope extraction and separation device which comprises an absorption tower, the absorption tower is provided with an absorption tower top condenser, an azeotrope feeding pipeline, an HFP discharging pipeline and an extraction agent discharging port, the extraction agent discharging port is communicated with a desorption tower condenser through a pipeline, the pipeline is provided with a circulating pump, the desorption tower condenser is communicated with a desorption tower through a pipeline, and the desorption tower is provided with a circulating pump. The desorption tower is communicated with a desorption tower condenser through a pipeline, the desorption tower condenser is communicated with an absorption tower cooler through a pipeline, the absorption tower cooler is communicated with an extracting agent feeding hole of the absorption tower through a pipeline, and two heat exchange pipelines in the desorption tower condenser are used for exchanging heat; a gas-phase material outlet of the desorption tower is communicated with a tower top condenser of the desorption tower, the tower top condenser of the desorption tower is communicated with a gas-phase material inlet of the desorption tower through a material return pipeline, and the material return pipeline is provided with an F22 discharge pipeline. According to the extraction separation device disclosed by the utility model, materials containing F22 / HFP are conveyed to the absorption tower, the relative volatility among components in an original mixture is changed by adding the extraction agent, and the absorbed F22 and HFP are released from the absorption agent in manners of heating, pressure reduction and the like and are recycled, so that efficient separation is realized, the production efficiency is further improved, and the production cost is reduced. The production cost is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to a kind of chlorodifluoromethane (F22) / hexafluoropropylene (HFP) azeotrope extraction separation devices, for separating hexafluoropropylene gas in chlorodifluoromethane (F22) / hexafluoropropylene (HFP) azeotrope, belong to chemical technology field. BACKGROUND

[0002] Hexafluoropropylene (HFP), also known as perfluoropropylene, is an organic compound with the chemical formula C3F6, which is a colorless gas at room temperature and pressure, insoluble in water, and is mainly used for manufacturing fluorine-containing fine chemicals, pharmaceutical intermediates, fire extinguishing agents and fluorine-containing polymer materials, etc. Chlorodifluoromethane (F22) is a stable chemical hydrogen-containing fluorine-chlorine hydrocarbon, with the chemical formula CHClF2, and its main uses include refrigerants, gas-soluble insecticide launchers, polytetrafluoroethylene resin raw materials, and intermediates for fire extinguishing agent 1121, etc.

[0003] In the production process of tetrafluoroethylene, chlorodifluoromethane (F22) / hexafluoropropylene (HFP) is prone to form azeotrope. The formation of this azeotrope is due to the constant boiling characteristics of these two gases under specific temperature and pressure conditions, which cannot be separated by conventional distillation or rectification methods. The existing chlorodifluoromethane (F22) / hexafluoropropylene (HFP) azeotrope extraction separation process has low separation efficiency, high energy consumption and high operating cost. SUMMARY

[0004] The purpose of the utility model is to provide a kind of F22 / HFP azeotrope extraction separation device, and the device F22 / HFP separation efficiency is high, and energy consumption and operating cost can be reduced.

[0005] In order to achieve the above technical purpose, the technical scheme of the utility model is:

[0006] The F22 / HFP azeotrope extraction separation device includes an absorption tower, an absorption tower overhead condenser is arranged at the top of the absorption tower, and the azeotrope feed inlet of the absorption tower is arranged at the middle and lower part of the absorption tower. The azeotrope feed inlet of the absorption tower is connected to the azeotrope feed pipeline, the HFP discharge port of the absorption tower is arranged at the top of the absorption tower, and the HFP discharge port of the absorption tower is connected to the HFP discharge pipeline.

[0007] The bottom of the absorption tower is provided with an extractant outlet, which is connected to the first condenser inlet of the desorption tower condenser through a first pipeline, the first pipeline is provided with a circulating pump, the first condenser outlet of the desorption tower condenser is connected to the first desorption tower inlet of the desorption tower through a second pipeline, the first desorption tower outlet of the desorption tower is connected to the second condenser inlet of the desorption tower condenser through a third pipeline, the second condenser outlet of the desorption tower condenser is connected to the cooler inlet of the absorption tower cooler through a fourth pipeline, the cooler outlet of the absorption tower cooler is connected to the extractant inlet of the absorption tower through a fifth pipeline, the absorption tower cooler cools the extractant, the first condenser inlet and the first condenser outlet of the desorption tower condenser are connected through a first heat exchange pipeline, the second condenser inlet and the second condenser outlet of the desorption tower condenser are connected through a second heat exchange pipeline, the first heat exchange pipeline and the second heat exchange pipeline exchange heat, the temperature in the first heat exchange pipeline is lower than the temperature in the second heat exchange pipeline, so as to cool the extractant in the second heat exchange pipeline.

[0008] The top of the desorption tower is provided with a gas phase material outlet and a gas phase material inlet, the gas phase material outlet of the desorption tower is connected to the gas phase material inlet of the desorption tower overhead condenser through a gas phase rising pipeline, the gas phase material outlet of the desorption tower overhead condenser is connected to the gas phase material inlet of the desorption tower through a back material pipeline, the desorption tower overhead condenser cools F22 in the gas phase rising pipeline, and the second back material pipeline is provided with an F22 outlet pipeline. By flowing part of the cooled F22 back to the desorption tower, the temperature in the desorption tower is reduced, and the purpose of controlling the temperature of the desorption tower is achieved.

[0009] The desorption tower is provided with an extractant; the extractant is methanol or water.

[0010] The absorption tower overhead condenser is provided with a constant-boiling substance outlet pipeline. By providing the constant-boiling substance outlet pipeline, the abnormal recovery of the extractive separation device is facilitated, and the safety risk is reduced.

[0011] The fifth pipeline is provided with a thermometer, and the temperature of the material in the fifth pipeline is detected by the thermometer to control the temperature of the material and ensure the absorption effect.

[0012] The fourth pipeline is provided with an adjusting valve, and the liquid level of the desorption tower is accurately controlled through the adjusting valve on the fourth pipeline to ensure the desorption effect.

[0013] The absorption tower and the desorption tower are both provided with a thermometer, a liquid level meter and a pressure gauge to realize the monitoring of the absorption tower 1 and the desorption tower 8.

[0014] The absorption tower and the desorption tower are both packed towers, and the packed tower is a silk screen corrugated packing.

[0015] The overhead condenser of the absorption tower is a single tube-pass shell-and-tube heat exchanger, and -35 DEG C refrigerant is used, and the absorption tower cooler and the condenser of the stripping tower are single tube-pass shell-and-tube heat exchangers, and -15 DEG C refrigerant is used.

[0016] In order to control the HFP discharge amount, the F22 discharge amount and the F22 / HFP azeotrope feed amount, the HFP discharge port of the absorption tower is provided with an adjusting valve and a flow meter, the F22 discharge pipeline is provided with an adjusting valve and a flow meter, and the azeotrope feed pipeline is provided with an adjusting valve and a flow meter.

[0017] The utility model discloses a precooling of extractant through the condenser of stripping tower, and then cooling the extractant through the absorption tower cooler again, which can effectively reduce energy consumption and device operation cost.

[0018] The utility model discloses an extraction separation device adopts the material containing F22 / HFP is transported to the absorption tower, changes the relative volatility between each component in the original mixture through adding extractant, and releases F22 and HFP from the absorbent through heating, pressure reduction and other modes, and recycling, thereby realizing efficient separation, and then improving production efficiency, reduce production cost. BRIEF DESCRIPTION OF DRAWINGS

[0019] The utility model will be further explained in detail in combination with the drawings and specific embodiment.

[0020] Figure 1 It is structure schematic drawing for the utility model. CONCRETE EMBODIMENT

[0021] As Figure 1 The utility model discloses an F22 / HFP azeotrope extraction separation device, which comprises an absorption tower 1, an absorption tower overhead condenser 14 arranged at the top of the absorption tower 1, an azeotrope discharge pipeline 15 arranged on the absorption tower overhead condenser 14, a control valve arranged on the azeotrope discharge pipeline 15, an HFP discharge port arranged at the top of the absorption tower 1, an HFP discharge pipeline 13 communicated with the HFP discharge port, an adjusting valve and a flow meter arranged on the HFP discharge pipeline 13, an azeotrope feed port arranged at the middle and lower part of the absorption tower 1, an azeotrope feed pipeline 2 communicated with the azeotrope feed port, and an adjusting valve and a flow meter arranged on the azeotrope feed pipeline 2.

[0022] The bottom of the absorption tower 1 is provided with an extractant outlet, which is connected to the first condensing tower inlet of the desorption tower condenser 6 through a first pipeline 3, the first pipeline 3 is provided with a circulating pump 5, the first condensing tower outlet of the desorption tower condenser 6 is connected to the first desorption tower inlet of the desorption tower 8 through a second pipeline 7, the first desorption tower outlet of the desorption tower 8 is connected to the second condensing tower inlet of the desorption tower condenser 6 through a third pipeline 9, the second condensing tower outlet of the desorption tower condenser 6 is connected to the cooler inlet of the absorption tower cooler 11 through a fourth pipeline 10, the cooler outlet of the absorption tower cooler 11 is connected to the extractant inlet of the absorption tower 1 through a fifth pipeline 12, the absorption tower cooler 11 cools the extractant, the first condensing tower inlet and the first condensing tower outlet of the desorption tower condenser 6 are connected through a first heat exchange pipeline, the second condensing tower inlet and the second condensing tower outlet of the desorption tower condenser are connected through a second heat exchange pipeline, the first heat exchange pipeline and the second heat exchange pipeline exchange heat, the material temperature in the first heat exchange pipeline is lower than the material temperature in the second pipeline, so as to cool the extractant in the second heat exchange pipeline.

[0023] The top of the desorption tower 8 is provided with a gas phase material outlet and a gas phase material inlet, the gas phase material outlet of the desorption tower 8 is connected to the gas phase material outlet of the desorption tower overhead condenser 17 through a gas phase rising pipeline 16, the gas phase material outlet of the desorption tower overhead condenser 17 is connected to the gas phase material inlet of the desorption tower 8 through a back material pipeline 18, the desorption tower overhead condenser 17 cools F22 in the gas phase rising pipeline 16, the back material pipeline 18 is provided with an F22 outlet pipeline 19, the F22 outlet pipeline 19 is provided with an adjusting valve and a flowmeter.

[0024] The desorption tower 8 is provided with an extractant, which is methanol or water.

[0025] The fifth pipeline 12 is provided with a thermometer, the material temperature in the fifth pipeline 12 is detected by the thermometer to control the material temperature and ensure the absorption effect.

[0026] The fourth pipeline 10 is provided with an adjusting valve, the liquid level of the desorption tower is accurately controlled by the adjusting valve on the fourth pipeline 10 to ensure the desorption effect.

[0027] The absorption tower 1 and the desorption tower 8 are both provided with a thermometer, a liquid level meter and a pressure gauge to monitor the absorption tower 1 and the desorption tower 8.

[0028] The absorption tower 1 and the desorption tower 8 are both packed towers, and the packed tower is a silk screen corrugated packing.

[0029] The absorption tower overhead condenser 14 is a single tube process shell and tube heat exchanger, which uses-35℃ refrigerant, the absorption tower cooler 11 and the desorption tower condenser 6 are single tube process shell and tube heat exchangers, which use-15℃ refrigerant.

[0030] In use, the constant-boiling substance is delivered into the absorption tower through the constant-boiling substance feeding pipeline 2, the extractant in the stripping tower 8 is delivered into the absorption tower 1 through the third pipeline 9, the stripping tower condenser 6, the fourth pipeline 10, the absorption tower cooler 11 and the fifth pipeline 12, the extractant absorbs F22 in the constant-boiling substance, the extractant absorbing F22 is delivered into the stripping tower 8 by the circulating pump 5 through the stripping tower condenser 6 and the second pipeline 7, the stripping tower 8 separates the extractant and F22, the separated F22 is delivered into the stripping tower overhead condenser 17 through the gas phase rising pipeline 16, a part of the F22 cooled by the stripping tower overhead condenser 17 is refluxed into the stripping tower through the reflux pipeline 18 to cool the stripping tower, and the other part is recycled through the F22 discharging pipeline 19; the HFP in the absorption tower 1 is recycled through the HFP discharging pipeline 13.

[0031] The embodiment can effectively reduce energy consumption and device operation cost by pre-cooling the extractant through the stripping tower condenser and then cooling the extractant again through the absorption tower cooler.

[0032] The embodiment of the extractive separation device delivers the material containing F22 / HFP into the absorption tower, changes the relative volatility between the components in the original mixture by adding the extractant, releases the absorbed F22 and HFP from the absorbent by heating and reducing pressure and recycles and utilizes them, thereby realizing efficient separation, improving production efficiency and reducing production cost.

[0033] The above embodiments do not limit the utility model in any way, and any technical solution obtained by equivalent replacement or equivalent transformation falls within the protection scope of the utility model.

Claims

1. An F22 / HFP azeotropic extraction and separation apparatus, characterized in that: The absorption tower includes an absorption tower top condenser. The azeotropic feed inlet of the absorption tower is located in the lower middle part of the tower and is connected to an azeotropic feed pipeline. The HFP outlet of the absorption tower is located at the top and is connected to an HFP outlet pipeline. An extractant outlet is located at the bottom of the absorption tower and is connected to the first condenser inlet of the desorption tower condenser via a first pipeline. A circulation pump is installed on the first condenser outlet of the desorption tower condenser. The first condenser outlet of the desorption tower condenser is connected to the first desorption tower inlet of the desorption tower via a second pipeline. The first desorption tower outlet of the desorption tower is connected to the second condenser inlet of the desorption tower condenser via a third pipeline. The second condenser outlet of the desorption tower condenser is connected to the cooler inlet of the absorption tower cooler via a fourth pipeline. The cooler outlet of the absorption tower cooler is connected to the extractant inlet of the absorption tower via a fifth pipeline. The absorption tower cooler cools the extractant. The first condenser inlet and outlet of the desorption tower condenser are connected via a first heat exchange pipeline. The second condenser inlet and outlet of the desorption tower condenser are connected via a second heat exchange pipeline. The first and second heat exchange pipelines exchange heat. The top of the desorption tower is provided with a gas phase material outlet and a gas phase material inlet. The gas phase material outlet of the desorption tower is connected to the gas phase material inlet of the top condenser of the desorption tower via a gas phase rise pipeline. The gas phase material outlet of the top condenser of the desorption tower is connected to the gas phase material inlet of the desorption tower via a return pipeline. The top condenser of the desorption tower cools the F22 in the gas phase rise pipeline. The return pipeline is provided with an F22 outlet pipeline. The desorption tower contains extractant.

2. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The extractant is methanol or water.

3. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The absorber is equipped with an azeotropic discharge pipeline at the top of the absorber.

4. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The fifth pipeline is equipped with a thermometer.

5. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The fourth pipeline is equipped with a regulating valve.

6. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: Both the absorption tower and the desorption tower are packed towers.

7. The F22 / HFP azeotropic extraction and separation apparatus according to claim 6, characterized in that: The packed tower is made of wire mesh corrugated packing.

8. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The absorber tower top condenser is a single-pass shell-and-tube heat exchanger using -35℃ refrigerant, and the absorber tower cooler and the desorption tower condenser are both single-pass shell-and-tube heat exchangers using -15℃ refrigerant.

9. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: The HFP outlet of the absorption tower is equipped with a regulating valve and a flow meter, the F22 outlet pipeline is equipped with a regulating valve and a flow meter, and the azeotropic feed pipeline is equipped with a regulating valve and a flow meter.

10. The F22 / HFP azeotropic extraction and separation apparatus according to claim 1, characterized in that: Both the absorption tower and the desorption tower are equipped with thermometers, level gauges, and pressure gauges.

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