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Method for coupling MTO process and naphtha and propane cracking progressive separation process

A technology of sequential separation and naphtha, applied in the direction of distillation purification/separation, hydrocarbon purification/separation, chemical instruments and methods, etc., can solve the problems of low benefit of raw material products, large investment, unreasonable process design, etc., and achieve reduction The effect of energy consumption, investment reduction and good technical effect

Active Publication Date: 2014-12-24
SINOPEC SHANGHAI ENG +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The technical problem to be solved by the present invention is the problem of unreasonable process design, large investment, and low benefit of raw material products in the existing coupling technology. It provides a new method for coupling the MTO process with the sequential separation process of naphtha and propane cracking

Method used

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  • Method for coupling MTO process and naphtha and propane cracking progressive separation process
  • Method for coupling MTO process and naphtha and propane cracking progressive separation process

Examples

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Effect test

Embodiment 1

[0022] The naphtha and propane steam cracking ethylene unit adopts a sequential separation process. The ethylene production capacity is 1.2 million tons / year, the propane raw material feed is 790,400 tons / year, and the mass ratio of propylene to ethylene in the cracking gas is 0.53. New The methanol processing scale of the MTO unit is 1.8 million tons per year, and the mass ratio of ethylene to propylene in the MTO product gas is 1.5. After the product gas of the MTO unit is separated and compressed in the rough separation tower, part of C3 and all lighter components are sent to the five-stage compression outlet of the cracking unit, and enter the cold box of the cracking unit together with the cracking gas; the product gas of the MTO unit is separated in the depropanizer Finally, the tower bottom liquid and the naphtha steam cracking ethylene plant's depropanizer bottom liquid enter the ethylene plant's debutanizer for separation. Using the coupling method of the present inve...

Embodiment 2

[0026] According to the conditions and steps described in Example 1, the ethylene production capacity of the naphtha and propane steam cracking ethylene plant is 1.1 million tons per year, and the specific data are shown in Table 1. Compared with Comparative Example 2, the input of naphtha is reduced by 2.2594 million tons / year, and the production of propylene is increased by 15,400 tons / year.

Embodiment 3

[0030] According to the conditions and steps described in Comparative Example 1, the ethylene production capacity of the naphtha and propane steam cracking ethylene plant is 1 million tons per year, and the mass ratio of ethylene to propylene in the product gas of the newly added MTO plant is 0.8. Using the coupling method described in the present invention, the operating conditions of the crude separation tower are: temperature is -20°C, and pressure is 0.6MPaG. See Table 1 for specific data. Compared with Comparative Example 3, 1.8263 million tons of naphtha was reduced per year, and propylene production was increased by 153.9 thousand tons per year.

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Abstract

The invention relates to a method for coupling an MTO process and a naphtha and propane cracking progressive separation process, and mainly aims to solve the problems of unreasonable process design, relatively large investment and relatively low raw material product benefit of an existing coupling technology. According to the technical scheme of the method for coupling the MTO process and the naphtha and propane cracking progressive separation process, MTO product gas is compressed and dried, and then enters a crude separation tower; an overhead stream of the crude separation tower including below C2 and partial C3 components enters an ice chest in the naphtha and propane cracking progressive separation process; a bottom stream of the crude separation tower including rest C3 and above C4 components enters a depropanizer in the MTO separation process; a bottom stream of the depropanizer enters a debutanizer in the naphtha and propane cracking progressive separation process. Therefore, the problems can be relatively well solved, and the method can be used for producing light olefins.

Description

technical field [0001] The invention relates to a method for coupling an MTO process with a sequential separation process of naphtha and propane cracking. Background technique [0002] Low-carbon olefins, namely ethylene and propylene, are two important basic chemical raw materials. At present, ethylene and propylene are mainly produced through petroleum routes, such as naphtha steam cracking technology to produce ethylene and propylene. US20070083071 discloses a process for producing ethylene and propylene by catalytic cracking of hydrocarbons. The hydrocarbon raw materials are converted into products including low-carbon olefins in a catalytic cracking furnace, and then the product stream is separated into C2~C3 alkanes, C2~C3 Olefins and C4+ hydrocarbons are three kinds of streams. C2~C3 alkanes are returned to the tubular cracking furnace for thermal cracking, and C4+ hydrocarbons are returned to the catalytic cracking furnace for catalytic cracking, and finally ethylene...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C7/00C07C7/04C07C4/02C07C11/04C07C11/06
CPCY02P30/20Y02P30/40
Inventor 张永生陈益徐蔚何琨
Owner SINOPEC SHANGHAI ENG
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