Front-end deethanizing separation process method for ethylene device

A technology of ethylene plant and process method, which is applied in the field of chemical engineering, and can solve problems such as rising low-pressure steam consumption and increasing heat load of deethanizer bottom reboiler

Active Publication Date: 2011-02-09
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The feed condensate temperature of the existing deethanizer tower in China is relatively low, generally lower than 13°C. After the condensate enters the mid...

Method used

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  • Front-end deethanizing separation process method for ethylene device
  • Front-end deethanizing separation process method for ethylene device
  • Front-end deethanizing separation process method for ethylene device

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0030] exist figure 2 Among them, the evaporation temperature of the condensate pre-heater E311 is selected to be 30°C, and the condensate heater E312 heats the process flow 33 to 60°C. implement the present invention figure 2 Example typical data are listed in Table 2. It can be seen from Table 2 that the implementation figure 2 After the invention, the cooling capacity required by the top condenser of the deethanizer was reduced by 10kw, the uncondensed gas flow rate was reduced by 456kg / h, and the final power of the cracked gas compressor was reduced by 16kw at the same time. implement figure 2After the invention, the ethylene unit further utilizes the surplus quench water heat to reduce the heat load of the reboiler at the bottom of the deethanizer and the circulating water volume for cooling the quench water. It can be seen from Tables 1 and 2 that the heat load of the reboiler at the bottom of the deethanizer decreased by 14410.8MJ / h, and the consumption of low-p...

Embodiment 2

[0034] exist image 3 Among them, the condensate pre-heater E311 is canceled, and the condensate heater E312 heats the process stream 33, 10 at 10.7°C to 50°C. implement the present invention image 3 Example typical data are listed in Table 3. As can be seen from Table 3, the implementation image 3 After the invention, the cooling capacity required by the top condenser of the deethanizer was reduced by 38kw, but the flow rate of uncondensed gas was increased by 206kg / h, and the power of the cracked gas compressor was increased by 5kw at the same time. The cooling capacity required by the pre-cooling section An increase of 9kw has little effect on cracked gas compressors and propylene refrigeration compressors. implement image 3 After the invention, it can be seen from Tables 1 and 3 that the heat load of the reboiler at the bottom of the deethanizer decreased by 11696.8MJ / h, and the consumption of low-pressure steam was reduced by 5023kg / h; the amount of circulating wat...

Embodiment 3

[0038] Will image 3 The condensate heater E312 in is moved to the deethanizer tower as an intermediate reboiler, and the heat load of the intermediate reboiler is the same as in Scheme 2 image 3 The heat load of the condensate heater E312 is the same in the example. After implementing this, with image 3 Compared with the typical data in Table 3 of the example, only the cooling data of the deethanizer overhead condenser increased from 38kw to 150kw, and other data remained almost unchanged, indicating that adding the middle reboiler of the deethanizer further reduced the Cooling capacity required by the tower overhead condenser. The comprehensive energy consumption per ton of ethylene produced by the ethylene plant decreased by 158MJ, that is, 3.78 kg standard oil / ton of ethylene.

[0039] According to the results of the examples, after applying the present invention, the comprehensive energy consumption per ton of ethylene produced by large and medium-sized ethylene plan...

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Abstract

The invention relates to a front-end deethanizing separation process method for an ethylene device. Liquid phase material flow from pyrolysis gas condensate drier is heated for evaporating in a condensate preheater by using chilled water at the evaporating temperature of between 25 and 35 DEG C, a small amount of evaporated gaseous phase material flow containing hydrogen, methane and carbon-2-components is merged with gaseous phase material flow formed by part of pre-cooled gaseous phase pyrolysis gas at the temperature of between -10 DEG C and -12 DEG C which flows into a plate heat exchanger directly from the pyrolysis gas drier, and the mixed material flow is conveyed to the plate heat exchanger to be pre-cooled; and after being subjected to throttling through a valve under the reducedpressure, condensate material flow from the bottom of the condensate preheater is heated again in the condensate heater by using the chilled water, and gas-liquid phase material flow at the temperature of between 45 and 65 DEG C is conveyed to the middle part of a deethanizing tower. Through the method, the low-pressure steam consumption of a reboiler at the tower bottom of the low-pressure deethanizing tower is reduced, the circulating water volume of the cooling chilled water is reduced, and the comprehensive energy consumption of ethylene per ton produced by the ethylene device is reduced by 125 to 190 MJ.

Description

technical field [0001] The invention belongs to the separation engineering technology in the ethylene production process in the field of chemical engineering, and relates to a separation process method for deethanization before double towers of an ethylene plant. Background technique [0002] The deethanization separation process before the double tower used in the domestic ethylene plant starts from the outlet of the cracked gas compressor (such as the fifth stage). After the cracked gas is compressed by the cracked gas compressor, the pressure reaches above 3.6MPa. First use circulating water to cool the cracked gas, and then use propylene refrigerant to cool it down to 15°C. After the gas-liquid separation of the cracked gas, the gas-phase stream is dried and then absorbed part of the cooling capacity of the process stream and propylene refrigerant in a plate heat exchanger to be continuously cooled, and the cooled stream is subjected to gas-liquid separation again, and ...

Claims

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Application Information

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IPC IPC(8): C07C7/00C07C11/04
Inventor 卢光明陈俊豪刘明辉林庆富龚树鹏
Owner PETROCHINA CO LTD
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