C4 extraction separation solvent regeneration energy-saving system

Abstract

The utility model relates to the technical field of chemical engineering, and discloses a C4 extraction separation solvent regeneration energy-saving system which comprises a light component removal tower system and a heavy component removal tower system, the light component removal tower system comprises a light component removal tower, a light component removal tower water cooler, a light component removal tower reflux tank, a light component removal tower reflux pump and a light component removal tower kettle delivery pump; the de-heavy tower system comprises a de-heavy tower, a de-heavy tower water cooler, a de-heavy tower reflux tank, a de-heavy tower reflux pump and a vacuum pump. A solvent from which intermediate component impurities are to be removed firstly enters a heavy component removal tower to be separated, nitrogen formylmorpholine and heavy components are separated from a tower kettle, tower top effluents are methyl ethyl ketone and intermediate components, methyl ethyl ketone and the intermediate components enter a light component removal tower to be separated, methyl ethyl ketone flows out of the light component removal tower top, and light component removal tower kettle liquid is the intermediate components, so that the intermediate components are removed; the temperatures of the light component removal tower kettle and the heavy component removal tower kettle are both 160 DEG C, and the steam pressure is 0.8 MPa, so that the requirements can be met, and the energy consumption is reduced.

Description

Technical Field

[0001] The utility model relates to the technical field of chemical industry, in particular to a C4 extraction and separation solvent regeneration and energy-saving system. Background Art

[0002] C4 extraction separates butene and butane using methyl ethyl ketone (MEK) and morpholine as solvents. During the production process, impurities are generated in the solvent system. Light components have boiling points lower than that of methyl ethyl ketone (MEK), intermediate components have boiling points higher than that of morpholine but lower than that of morpholine, and heavy components have boiling points higher than that of morpholine. As the proportion of impurities in the solvent increases, the C4 extraction separation efficiency is affected, energy consumption increases, and solvent regeneration is required. The current solvent regeneration process first passes the solvent through a lightness removal column to remove the methyl ethyl ketone from the top. The intermediate components, morpholine, and other components in the bottom of the column are then pumped to a heaviness removal column. Under negative pressure in the heaviness removal column, the intermediate components and morpholine are separated, and the intermediate components are removed from the top of the column, leaving morpholine as the bottom. Due to the high boiling points of the components in the lightness removal and heaviness removal column bottoms, the bottom temperature must be above 190°C, requiring a steam pressure of 1.6 MPa. Steam is continuously used in both the lightness removal and heaviness removal columns throughout the regeneration process, resulting in significant energy consumption. Utility Model Content

[0003] The purpose of the utility model is to overcome the shortcomings of the prior art and provide a C4 extraction and separation solvent regeneration energy-saving system.

[0004] In order to achieve the above-mentioned purpose, the technical solution of the utility model is: a carbon four extraction separation solvent regeneration energy-saving system, comprising a light removal tower system and a heavy removal tower system; the light removal tower system comprises a light removal tower, a light removal tower water cooler, a light removal tower kettle reboiler, a light removal tower reflux tank, a light removal tower reflux pump, and a light removal tower kettle external delivery pump; the heavy removal tower system comprises a heavy removal tower, a heavy removal tower water cooler, a heavy removal tower reflux tank, a heavy removal tower reflux pump, and a vacuum pump;

[0005] The feed port of the weight-removing tower is connected to the feed pipeline, the gas phase outlet at the top of the weight-removing tower is connected to the weight-removing tower water cooler and the weight-removing tower reflux tank in sequence, the bottom outlet of the weight-removing tower reflux tank is connected to the weight-removing tower reflux pump, the outlet of the weight-removing tower reflux pump is connected to two pipelines, one of which is connected to the reflux port at the top of the weight-removing tower, and the other is connected to the feed port of the light-removing tower. A branch line is connected to the outlet pipeline of the weight-removing tower reflux tank, the two inlets of the vacuum pump are respectively connected to the branch line and the non-condensable gas port of the weight-removing tower water cooler, the outlet of the vacuum pump is connected to the gas phase port of the weight-removing tower reflux tank, and the outlet of the weight-removing tower kettle enters the solvent tank through a pipeline;

[0006] The gas phase outlet at the top of the light-removal tower is connected to the light-removal tower water cooler and the light-removal tower reflux tank in sequence, the outlet of the light-removal tower reflux tank is connected to the inlet of the light-removal tower reflux pump, the outlet of the light-removal tower reflux pump is connected to two pipelines, one of which is connected to the reflux port at the top of the light-removal tower, and the other pipeline enters the solvent tank, the outlet of the light-removal tower kettle is connected to the light-removal tower kettle external delivery pump, and the outlet of the light-removal tower kettle external delivery pump enters the dirty oil tank through a pipeline.

[0007] Furthermore, the light removal tower kettle is connected to a light removal tower kettle reboiler to provide a heat source for vaporization of the light removal tower material.

[0008] Furthermore, a delivery pump cooler is provided on the outlet pipeline of the light removal tower kettle delivery pump.

[0009] Furthermore, the deweighting tower kettle is connected to a deweighting tower kettle reboiler to provide a heat source for vaporization of the deweighting tower material.

[0010] Furthermore, the outlet pipeline of the deweighting tower kettle is connected to a deweighting tower inlet and outlet heat exchanger, and another pipeline of the deweighting tower reflux pump outlet passes through the deweighting tower inlet and outlet heat exchanger and is connected to the delighting tower feed port.

[0011] Furthermore, the top outlet of the deweighting tower reflux tank is connected to a vent line to flare venting.

[0012] The beneficial effects of the utility model are as follows: the solvent from which the intermediate component impurities are to be removed first enters a de-weighting tower for separation, the tower bottom separates nitrogen methyl morpholine and heavy components, the tower top outflow is methyl ethyl ketone and intermediate components, the methyl ethyl ketone and intermediate components then enter a de-lighting tower for separation, methyl ethyl ketone flows out from the top of the de-lighting tower, and the de-lighting tower bottom liquid is the intermediate components, thereby achieving the removal of the intermediate components. The solvent from which the intermediate component impurities are to be removed has a high boiling point, and separation in a de-weighting tower in a negative pressure environment reduces the boiling point temperature, the de-lighting tower feed components become methyl ethyl ketone and intermediate components, reducing the boiling point temperature of the de-lighting tower material, the tower bottom temperature of the de-lighting tower and the tower bottom temperature of the de-weighting tower are both 160°C, which can be met by a steam pressure of 0.8MPa, thereby reducing the quality of steam and reducing energy consumption. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] Figure 1 It is a system diagram of the utility model.

[0014] In the figure: 1. Light-removal tower; 2. Reboiler of the kettle of light-removal tower; 3. Water cooler of light-removal tower; 4. Reflux tank of light-removal tower; 5. Reflux pump of light-removal tower; 6. External pump of kettle of light-removal tower; 7. Cooler of external pump; 8. Heavy-removal tower; 9. Reboiler of kettle of heavy-removal tower; 10. Water cooler of heavy-removal tower; 11. Reflux tank of heavy-removal tower; 12. Reflux pump of heavy-removal tower; 13. Vacuum pump; 14. Inlet and outlet heat exchanger of heavy-removal tower. DETAILED DESCRIPTION

[0015] Example:

[0016] like Figure 1 As shown, a carbon four extraction and separation solvent regeneration and energy-saving system includes a light removal tower system and a heavy removal tower system; the light removal tower system includes a light removal tower 1, a light removal tower kettle reboiler 2, a light removal tower water cooler 3, a light removal tower reflux tank 4, a light removal tower reflux pump 5, and a light removal tower kettle external delivery pump 6; the heavy removal tower system includes a heavy removal tower 8, a heavy removal tower water cooler 10, a heavy removal tower reflux tank 11, a heavy removal tower reflux pump 12, a vacuum pump 13, and a heavy removal tower inlet and outlet heat exchanger 14.

[0017] The feed port of the deweighting tower 8 is connected to the feed pipeline, the kettle of the deweighting tower 8 is connected to the deweighting tower kettle reboiler 9, the outlet pipeline of the kettle of the deweighting tower 8 is connected to the deweighting tower inlet and outlet heat exchanger 14 and then enters the solvent tank, the gas phase outlet at the top of the deweighting tower 8 is connected to the deweighting tower water cooler 10 and the deweighting tower reflux tank 11 in sequence, the bottom outlet of the deweighting tower reflux tank 11 is connected to the deweighting tower reflux pump 12, and the top outlet of the deweighting tower reflux tank 11 is connected to the vent pipeline To vent the flare, the outlet of the de-weighting tower reflux pump 12 is connected to two pipelines, one of which is connected to the reflux port at the top of the de-weighting tower 8, and the other is connected to the feed port of the de-lightening tower 1 after passing through the de-weighting tower inlet and outlet heat exchanger 14. A branch line is connected to the outlet pipeline of the de-weighting tower reflux tank 11, and the two inlets of the vacuum pump 13 are respectively connected to the branch line and the non-condensable gas port of the de-weighting tower water cooler 10, and the outlet of the vacuum pump 13 is connected to the gas phase port of the de-weighting tower reflux tank 11.

[0018] The gas phase outlet at the top of the light-removing tower 1 is connected in sequence to the light-removing tower water cooler 3 and the light-removing tower reflux tank 4, the outlet of the light-removing tower reflux tank 4 is connected to the inlet of the light-removing tower reflux pump 5, the outlet of the light-removing tower reflux pump 5 is connected to two pipelines, one of which is connected to the reflux port at the top of the light-removing tower 1, and the other pipeline enters the solvent tank, the tower kettle of the light-removing tower 1 is connected to the light-removing tower kettle reboiler 2, the tower kettle outlet of the light-removing tower 1 is connected to the light-removing tower kettle external delivery pump 6, the outlet of the light-removing tower kettle external delivery pump 6 enters the dirty oil tank through a pipeline, and the outlet pipeline of the light-removing tower kettle external delivery pump 6 is provided with an external delivery pump cooler 7.

[0019] Working principle: The deweighting tower 8 is a negative pressure tower, and the pressure of the deweighting tower is controlled by the vacuum pump 13 at -0.062MPa. The solvent to be removed from the intermediate component impurities at 160°C enters the deweighting tower 8 for separation. The top effluent is methyl ethyl ketone and intermediate components. After being cooled by the deweighting tower water cooler 10, it enters the deweighting tower reflux tank 11. The top effluent coolant is pumped out by the deweighting tower reflux pump 12. Part of it is used as reflux of the deweighting tower 8, and the other part is sent out as feed for the lightness removal tower 1. The kettle liquid of the deweighting tower 8 is nitrogen methyl ethyl ketone and heavy components. The liquid in the kettle of the de-weighting tower 8 flows out by self-pressure, exchanges heat with the liquid sent from the top of the tower through the de-weighting tower inlet and outlet heat exchanger 14, and then flows into the solvent tank. At the same time, the liquid sent from the top of the tower enters the de-lighting tower 1 for separation after heat exchange. Methyl ethyl ketone flows out from the top of the de-lighting tower 1, is cooled by the de-lighting tower water cooler 3, and then enters the de-lighting tower reflux tank 4. It is pumped out through the de-lighting tower reflux pump 5. Part of it is used as the reflux of the de-lighting tower 1, and part of it is sent to the solvent tank, mixed with the liquid in the kettle of the de-weighting tower 8, and sent back to the solvent system. The liquid in the kettle of the de-lighting tower 1 is the intermediate component, which is intermittently sent out through the de-lighting tower kettle sending pump 6. The temperature of the tower kettle of the de-lighting tower and the tower kettle of the de-weighting tower are both 160℃, and the steam pressure of 0.8MPa can meet the requirements.

[0020] The above-described embodiments are only preferred solutions of the present invention and do not limit the present invention in any form. Other variations and modifications are possible without exceeding the technical solutions described in the claims.

[0021] In the description of the present invention, it should be understood that the terms indicating orientation or positional relationships are based on the orientation or positional relationships shown in the accompanying drawings, and are only for the convenience of describing the present invention and simplifying the description, and 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. Therefore, it cannot be understood as a limitation on the present invention.

Claims

1. A C4 extraction and separation solvent regeneration and energy-saving system, characterized by: It comprises a lightness removal tower system and a heavyness removal tower system; the lightness removal tower system comprises a lightness removal tower (1), a lightness removal tower kettle reboiler (2), a lightness removal tower water cooler (3), a lightness removal tower reflux tank (4), a lightness removal tower reflux pump (5), and a lightness removal tower kettle external delivery pump (6); the heavyness removal tower system comprises a heavyness removal tower (8), a heavyness removal tower water cooler (10), a heavyness removal tower reflux tank (11), a heavyness removal tower reflux pump (12), and a vacuum pump (13); The feed port of the deweighting tower (8) is connected to the feed pipeline, the gas phase outlet at the top of the deweighting tower (8) is connected to the deweighting tower water cooler (10) and the deweighting tower reflux tank (11) in sequence, the bottom outlet of the deweighting tower reflux tank (11) is connected to the deweighting tower reflux pump (12), the outlet of the deweighting tower reflux pump (12) is connected to two pipelines, one of which is connected to the reflux port at the top of the deweighting tower (8), and the other is connected to the feed port of the delightening tower (1), the outlet pipeline of the deweighting tower reflux tank (11) is connected to a branch line, the two inlets of the vacuum pump (13) are respectively connected to the branch line and the non-condensable gas port of the deweighting tower water cooler (10), the outlet of the vacuum pump (13) is connected to the gas phase port of the deweighting tower reflux tank (11), and the outlet of the kettle of the deweighting tower (8) enters the solvent tank through a pipeline; The gas phase outlet at the top of the light-removal tower (1) is connected to the light-removal tower water cooler (3) and the light-removal tower reflux tank (4) in sequence; the outlet of the light-removal tower reflux tank (4) is connected to the inlet of the light-removal tower reflux pump (5); the outlet of the light-removal tower reflux pump (5) is connected to two pipelines, one of which is connected to the reflux port at the top of the light-removal tower (1), and the other is connected to the solvent tank; the outlet of the tower kettle of the light-removal tower (1) is connected to the light-removal tower kettle external delivery pump (6); the outlet of the light-removal tower kettle external delivery pump (6) is connected to the dirty oil tank through a pipeline.

2. The C4 extraction and separation solvent regeneration and energy-saving system according to claim 1, characterized in that: The tower kettle of the light removal tower (1) is connected to a tower kettle reboiler (2).

3. The C4 extraction and separation solvent regeneration and energy-saving system according to claim 1, characterized in that: An outlet pump cooler (7) is provided on the outlet pipeline of the light removal tower kettle outlet pump (6).

4. The C4 extraction and separation solvent regeneration and energy-saving system according to claim 1, characterized in that: The deweighting tower (8) kettle is connected to a deweighting tower kettle reboiler (9).

5. The C4 extraction and separation solvent regeneration and energy-saving system according to claim 1, characterized in that: The outlet pipeline of the de-weighting tower (8) kettle is connected to a de-weighting tower inlet and outlet heat exchanger (14), and another outlet pipeline of the de-weighting tower reflux pump (12) passes through the de-weighting tower inlet and outlet heat exchanger (14) and is connected to the feed port of the de-lighting tower (1).

6. The C4 extraction and separation solvent regeneration and energy-saving system according to claim 1, characterized in that: The top outlet of the deweighting tower reflux tank (11) is connected to a venting pipeline to vent to a flare.

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