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Method for lowering fuel consumption in methanol to propylene reaction system

A methanol-to-propylene and reaction system technology, applied in the direction of producing hydrocarbons from oxygen-containing organic compounds, can solve the problem of high energy consumption, achieve the effects of reducing workload, good technical effects, and reducing fuel consumption

Inactive Publication Date: 2015-02-04
SINOPEC SHANGHAI ENG +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The technical problem to be solved by the present invention is the problem of high energy consumption in the prior art, and a new method for reducing fuel consumption in the methanol-to-propylene reaction system is provided

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0018] The invention utilizes the residual heat of the methanol-to-propylene reaction mixture gas at the outlet of the methanol-to-propylene reactor to heat the reaction mixture gas at the outlet of the DME reactor, simultaneously vaporizes and superheats the methanol raw material, and the nominal production capacity of the methanol-to-propylene device is 500,000 tons / year of propylene. Methanol feed temperature is 90 DEG C, pressure is 1.40MPaG, temperature is 250 DEG C, pressure is 1.60MPaG after entering methanol vaporization superheating section; After the heating furnace is heated to 460°C, it enters the methanol-to-propylene reactor, 51.5% enters the dimethyl ether reaction gas superheating section, and the temperature is 460°C, and is sent to the methanol-to-propylene reactor, and the methanol-to-propylene product gas at the outlet of the methanol-to-propylene reactor The temperature is 480°C. The temperature of the methanol-to-propylene product gas after heat recovery ...

Embodiment 2

[0020] According to the conditions described in Example 1, the nominal production capacity of the methanol-to-propylene plant is 500,000 tons / year of propylene, but the operating conditions are changed. Methanol feed temperature is 102 ℃, pressure is 1.80MPaG, after entering the methanol vaporization superheating section, temperature is 265 ℃, pressure is 1.80MPaG; After the heating furnace is heated to 460°C, it enters the methanol-to-propylene reactor, and 57.4% enters the dimethyl ether reaction gas superheating section, and then the temperature is 466°C and is sent to the methanol-to-propylene reactor. The temperature of the methanol-to-propylene product gas at the outlet of the methanol-to-propylene reactor is It is 483°C. The temperature of the methanol-to-propylene product gas after heat recovery is 185-195°C. Since the DME reaction product stream is heated in the dimethyl ether reaction gas superheating section, 2199 kg / hour of natural gas fuel can be saved, which can...

Embodiment 3

[0022] According to the conditions described in Example 1, the nominal production capacity of the methanol-to-propylene plant is 500,000 tons / year of propylene, but the operating conditions are changed. Methanol feed temperature is 120 DEG C, pressure is 2.40MPaG, temperature is 280 DEG C, pressure is 1.90MPaG after entering methanol vaporization superheating section; After the heating furnace is heated to 460°C, it enters the methanol-to-propylene reactor, and 68.5% enters the dimethyl ether reaction gas superheating section, and then the temperature is 470°C and is sent to the methanol-to-propylene reactor. The temperature of the methanol-to-propylene product gas at the outlet of the methanol-to-propylene reactor is It is 490°C. The temperature of the methanol-to-propylene product gas after heat recovery is 180-185°C. Since the DME reaction product stream is heated in the superheating section of the dimethyl ether reaction gas, 2475 kg / hour of natural gas fuel can be saved,...

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PUM

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Abstract

The invention relates to a method of lowering fuel consumption in a methanol to propylene reaction system, and is mainly used for solving the problem that the energy consumption in the prior art is relatively high. The problem is well solved by the technical scheme that the method of lowering fuel consumption in the methanol to propylene reaction system comprises the following steps: introducing a methanol raw material into a methanol vaporization superheat section, introducing the heated methanol raw material into a dimethyl ether reactor, dividing material flow at the outlet of the dimethyl ether reactor into two parts, heating 30-50% (mass fraction) of the material flow by a heating furnace and then introducing the heated material flow into a methanol to propylene reactor, introducing 50-70% (mass fraction) of the material flow into a dimethyl ether reaction gas superheat section, introducing 50-70% of the material flow which is heated into the methanol to propylene reactor, feeding the methanol to propylene product gas in the outlet of the methanol to propylene reactor into the dimethyl ether reaction gas superheat section and the methanol vaporization superheat section in sequence, and feeding the heat-recycled methanol to propylene product gas into a separating unit. The method disclosed by the invention can be used for a methanol to propylene device.

Description

technical field [0001] The invention relates to a method for reducing fuel consumption in a methanol-to-propylene reaction system. Background technique [0002] Methanol to propylene technology refers to the process technology of producing propylene through catalytic reaction using coal-based or natural gas-based synthetic methanol as raw material. [0003] CN201310251451.8 relates to a low-energy-consumption propylene production process. It discloses that the raw material methanol is mixed with dilution gas to carry out etherification reaction. Carry out the reaction to prepare olefins to obtain secondary products, and then separate the secondary products from olefins to obtain propylene, ethylene and other products. After the separated process water is vaporized and returned to the reaction part as part of steam water, the separated ethylene, C1- C2 alkanes and C4-C6 products are also returned to the reaction part as refractory hydrocarbons. This patent achieves the goal ...

Claims

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Application Information

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IPC IPC(8): C07C1/20C07C11/06
Inventor 李真泽张红沈俊徐尔玲何琨
Owner SINOPEC SHANGHAI ENG