A system for the production of ethylene glycol

Abstract

The utility model provides a kind of production system of ethylene glycol, including reaction component, absorption tower and analytical tower, the first import of absorption tower is communicated with the first export of reaction component by first pipeline, analytical tower has first import and second import, the first import of analytical tower is communicated with the first export of absorption tower by second pipeline, and the second import of analytical tower is communicated with the second export of reaction component by third pipeline;Wherein, gas-liquid separation tank for buffering condensate is arranged on third pipeline, the utility model's beneficial effects:the production system of ethylene glycol proposed in the utility model, by setting gas-liquid separation tank, the acid, aldehyde and chlorine-containing solution generated in reaction component due to side reaction are discharged into gas-liquid separation tank, avoid the situation of corrosion equipment, corrosion pipeline, and by gas-liquid separation tank input into analytical tower, can prevent high pressure from straying low pressure during routine operation, avoid causing overpressure explosion.

Description

Technical Field

[0001] This utility model relates to the field of ethylene glycol production technology, and in particular to an ethylene glycol production system. Background Technology

[0002] The oxidation of ethylene to ethylene glycol is a core process in the chemical industry, and its technological evolution is closely linked to industrial needs. The traditional process uses ethylene as a raw material, which is oxidized by silver catalysis to produce ethylene oxide, which is then hydrated to produce ethylene glycol.

[0003] In the oxidation reaction of oxygen and ethylene, some of the water generated by the side reaction (deep oxidation) is cooled and condensed by the preheated tube gas. The condensate accumulates at the bottom of the heat exchanger. Over time, this accumulation will absorb acids, aldehydes, and chlorine-containing solutions generated by the side reaction in the circulating gas, thereby corroding the equipment and affecting the quality of ethylene glycol products. Currently, to avoid this drawback, operators manually drain the condensate at the bottom of the heat exchanger to the ethylene oxide stripping tower every 12 hours, which is a cumbersome operation. Furthermore, if the accumulated liquid in the heat exchanger is drained, the circulating gas (1.8 MPa) will leak into the ethylene oxide stripping tower (26 kPa), posing a risk of high pressure escalation into low pressure. Utility Model Content

[0004] This invention provides an ethylene glycol production system to solve the technical problems of condensate accumulating at the bottom of the heat exchanger, corroding the equipment and affecting the quality of ethylene glycol products, and the risk of high-pressure leakage to low-pressure areas if the accumulated liquid in the heat exchanger is drained.

[0005] This utility model provides an ethylene glycol production system, comprising: A reaction assembly having a first outlet and a second outlet; An absorption tower having a first outlet and a first inlet, wherein the first inlet of the absorption tower is connected to the first outlet of the reaction assembly via a first pipe; The analysis tower has a first inlet and a second inlet. The first inlet of the analysis tower is connected to the first outlet of the absorption tower through a second pipe, and the second inlet of the analysis tower is connected to the second outlet of the reaction assembly through a third pipe. The third pipeline is equipped with a gas-liquid separator for buffering condensate.

[0006] In one embodiment of the present invention, the production system further includes a first recovery pipe, the absorption tower has a second inlet, the desorption tower also has a first outlet, and the first outlet of the desorption tower and the second inlet of the absorption tower are connected through the first recovery pipe.

[0007] In one embodiment of the present invention, the production system further includes a second recovery pipe, and the gas-liquid separator is connected to the first pipe through the second recovery pipe.

[0008] In one embodiment of the present invention, the production system further includes a first heat exchanger, wherein both the first pipe and the second pipe pass through the first heat exchanger and exchange heat through the first heat exchanger.

[0009] In one embodiment of the present invention, the production system further includes a separation pipe and a water treatment component, one end of the separation pipe being connected to the first recovery pipe, and the other end of the separation pipe being connected to the water treatment component.

[0010] In one embodiment of the present invention, the production system further includes a hydration component, and the analysis tower also has a second outlet. The hydration component is connected to the second outlet of the analysis tower via a fourth pipe.

[0011] In one embodiment of the present invention, the third pipeline is provided with a control valve and a detection element for detecting the flow rate of the third pipeline, and the control valve is electrically connected to the detection element.

[0012] In one embodiment of this utility model, both the control valve and the detection element are located between the gas-liquid separator and the analytical tower.

[0013] In one embodiment of the present invention, the production system further includes a second heat exchanger, wherein both the first recovery pipe and the second pipe pass through the second heat exchanger and exchange heat within the second heat exchanger.

[0014] In one embodiment of the present invention, the production system further includes an evaporation component, which is connected to the water treatment component via a fifth pipe, and the evaporation component is connected to the hydration component via a sixth pipe.

[0015] The beneficial effects of this utility model are as follows: The ethylene glycol production system proposed in this utility model, by setting up a gas-liquid separator, discharges the acid, aldehyde and chlorine-containing solution generated by the side reaction in the reaction components into the gas-liquid separator, thereby avoiding corrosion of equipment and pipelines. Moreover, by inputting the gas-liquid separator into the desorption tower, it can prevent high pressure from crossing low pressure during daily operation and avoid overpressure explosion. Attached Figure Description

[0016] The accompanying drawings, which are incorporated in and form part of this specification, illustrate embodiments consistent with this application and, together with the description, serve to explain the principles of this application. It is obvious that the drawings described below are merely some embodiments of this application, and those skilled in the art can obtain other drawings based on these drawings without any inventive effort.

[0017] In the attached diagram: Figure 1 This is a schematic diagram of the system structure provided in an embodiment of the present utility model.

[0018] The attached figures are labeled as follows: 1. Absorption tower; 2. Desorption tower; 3. Third heat exchanger; 4. First pipeline; 5. Second pipeline; 6. Third pipeline; 7. Gas-liquid separator; 8. First recovery pipeline; 9. Second recovery pipeline; 10. First heat exchanger; 11. Separation pipeline; 12. Hydration assembly; 13. Second heat exchanger; 14. Water treatment assembly; 15. Evaporation assembly; 16. Fifth pipeline; 17. Sixth pipeline. Detailed Implementation

[0019] The following specific examples illustrate the implementation of this utility model. Those skilled in the art can easily understand other advantages and effects of this utility model from the content disclosed in this specification. This utility model can also be implemented or applied through other different specific embodiments. Various details in this specification can also be modified or changed based on different viewpoints and applications without departing from the spirit of this utility model. In the absence of conflict, the following embodiments and features in the embodiments can be combined with each other.

[0020] It should be noted that the illustrations provided in the following embodiments are only schematic representations of the basic concept of the present invention. The drawings only show the components related to the present invention and are not drawn according to the actual number, shape and size of the components. In actual implementation, the form, quantity and proportion of each component can be arbitrarily changed, and the layout of the components may also be more complex.

[0021] In the following description, numerous details are explored to provide a more thorough explanation of embodiments of the present invention. However, it will be apparent to those skilled in the art that embodiments of the present invention may be practiced without these specific details. In other embodiments, well-known structures and devices are shown in block diagram form rather than in detail to avoid obscuring embodiments of the present invention.

[0022] Please see Figure 1 , Figure 1An embodiment of the present invention provides an ethylene glycol production system, comprising a reaction assembly, an absorption tower 1, and a stripping tower 2. The reaction assembly has a first outlet and a second outlet, and includes a third heat exchanger 3. Both the first and second outlets pass through the third heat exchanger 3. Ethylene oxide enters a first pipe 4 through the first outlet and finally enters the absorption tower 1. The absorption tower 1 has a first outlet and a first inlet. The first inlet of the absorption tower 1 is connected to the first outlet of the reaction assembly through the first pipe 4. The stripping tower 2 has a first inlet and a second inlet. The first inlet of the stripping tower 2 is connected to the first outlet of the absorption tower 1 through a second pipe 5, and the second inlet of the stripping tower 2 is connected to the second outlet of the reaction assembly through a third pipe 6. After being processed by the absorption tower 1, the ethylene oxide enters the stripping tower 2 and is finally produced as ethylene glycol after stripping. Among them, the third pipeline 6 is equipped with a gas-liquid separator 7. The by-product liquid generated at the bottom of the third heat exchanger 3 is discharged into the gas-liquid separator 7, which can prevent the condensate from accumulating for a long time and absorbing the acid, aldehyde and chlorine-containing solution generated by the side reaction in the circulating gas, thus avoiding the corrosion of equipment and pipelines. Moreover, the gas-liquid separator 7 is fed into the desorption tower 2 to prevent high pressure from crossing to low pressure and avoid overpressure explosion.

[0023] Specifically, in an optional embodiment of this application, the production system further includes a first recovery pipe 8, the absorption tower 1 has a second inlet, and the desorption tower 2 has a first outlet. The first outlet of the desorption tower 2 and the second inlet of the absorption tower 1 are connected through the first recovery pipe 8, which can return the gas and liquid that have not been completely converted into ethylene glycol in the desorption tower 2 to the absorption tower 1 for reprocessing, so that it can be transported back to the desorption tower 2 for desorption after processing, thereby improving the conversion rate and increasing the production volume of the product and avoiding waste.

[0024] Specifically, in an optional embodiment of this application, the production system further includes a second recovery pipe 9, and the gas-liquid separator 7 also has the function of separating gas and liquid. The top of the gas-liquid separator 7 is provided with a gas outlet, and the gas outlet of the gas-liquid separator 7 is connected to the first pipe 4 through the second recovery pipe 9 to recover the effective gas phase, and the ethylene oxide in the gas-liquid separator 7 is separated again into the absorption tower 1 for processing, thereby improving production efficiency.

[0025] Specifically, in an optional embodiment of this application, a first heat exchanger 10 is also included. The first pipe 4 and the second pipe 5 are both set through the first heat exchanger 10 and exchange heat through the first heat exchanger. Ethylene oxide is preheated before entering the desorption tower 2, resulting in better desorption effect.

[0026] Specifically, in an optional embodiment of this application, the production system further includes a separation pipe 11 and a water treatment component 14. One end of the separation pipe 11 is connected to the first recovery pipe 8, and the other end of the separation pipe 11 is connected to the water treatment component 14, for removing waste liquid from the first recovery pipe 8 and performing water treatment to further extract ethylene glycol or ethylene oxide from the waste liquid.

[0027] Specifically, in an optional embodiment of this application, the production system further includes a hydration component 12, and the stripping tower 2 also has a second outlet. The hydration component 12 is connected to the second outlet of the stripping tower 2 through a fourth pipe. The ethylene oxide stripped by the stripping tower 2 enters the hydration component 12, reacts to produce ethylene glycol, and finally enters the purification component to produce purified ethylene glycol.

[0028] Specifically, in one optional embodiment of this application, a control valve and a detection element for detecting the flow rate of the third pipeline 6 are provided on the third pipeline 6. The control valve and the detection element are electrically connected. Both the control valve and the detection element are located between the gas-liquid separator 7 and the desorption tower 2. By detecting the flow rate in the third pipeline 6, the control valve acts as a flow regulating valve, thereby regulating the opening and closing of the control valve to ensure that condensate does not accumulate in the third heat exchanger 3, further preventing the risk of high pressure crossing into low pressure.

[0029] Specifically, in an optional embodiment of this application, the production system further includes a second heat exchanger 13, and both the first recovery pipe 8 and the second pipe 5 pass through the second heat exchanger 13, where the first recovery pipe 8 and the second pipe 5 exchange heat.

[0030] Specifically, in an optional embodiment of this application, the production system further includes an evaporation component 15, which is connected to the water treatment component 14 via a fifth pipe 16 and is connected to the hydration component 12 via a sixth pipe 17 to further refine the ethylene glycol and simultaneously refine the waste liquid treated by the water treatment component 14, thereby saving materials and improving product production efficiency.

[0031] The above embodiments are merely illustrative of the principles and effects of this utility model and are not intended to limit the scope of this utility model. Any person skilled in the art can modify or alter the above embodiments without departing from the spirit and scope of this utility model. Therefore, all equivalent modifications or alterations made by those skilled in the art without departing from the spirit and technical concept disclosed in this utility model should still be covered by the claims of this utility model.

Claims

1. A system for producing ethylene glycol, characterized in that, include: A reaction assembly having a first outlet and a second outlet; An absorption tower having a first outlet and a first inlet, wherein the first inlet of the absorption tower is connected to the first outlet of the reaction assembly via a first pipe; The analysis tower has a first inlet and a second inlet. The first inlet of the analysis tower is connected to the first outlet of the absorption tower through a second pipe, and the second inlet of the analysis tower is connected to the second outlet of the reaction assembly through a third pipe. The third pipeline is equipped with a gas-liquid separator for buffering condensate.

2. The ethylene glycol production system according to claim 1, characterized in that: The production system also includes a first recovery pipeline, the absorption tower has a second inlet, the desorption tower also has a first outlet, and the first outlet of the desorption tower and the second inlet of the absorption tower are connected through the first recovery pipeline.

3. The ethylene glycol production system according to claim 1, characterized in that: The production system also includes a second recovery pipeline, through which the gas-liquid separator is connected to the first pipeline.

4. The ethylene glycol production system according to claim 1, characterized in that: The production system also includes a first heat exchanger, through which both the first pipe and the second pipe pass and exchange heat.

5. The ethylene glycol production system according to claim 2, characterized in that: The production system also includes a separation pipe and a water treatment component. One end of the separation pipe is connected to the first recovery pipe, and the other end of the separation pipe is connected to the water treatment component.

6. The ethylene glycol production system according to claim 5, characterized in that: The production system also includes a hydration component, and the desorption tower has a second outlet. The hydration component is connected to the second outlet of the desorption tower via a fourth pipe.

7. The ethylene glycol production system according to claim 1, characterized in that: The third pipeline is equipped with a control valve and a detection device for detecting the flow rate of the third pipeline, and the control valve is electrically connected to the detection device.

8. The ethylene glycol production system according to claim 7, characterized in that: Both the control valve and the detection device are located between the gas-liquid separator and the analytical tower.

9. The ethylene glycol production system according to claim 2, characterized in that: The production system also includes a second heat exchanger, through which both the first recovery pipe and the second pipe pass and exchange heat.

10. The ethylene glycol production system according to claim 6, characterized in that: The production system also includes an evaporation component, which is connected to the water treatment component via a fifth pipe, and is connected to the hydration component via a sixth pipe.

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