Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds

A compound and olefin technology, applied in the production of hydrocarbons from oxygen-containing organic compounds, feed devices, chemical/physical/physical-chemical nozzle reactors, etc. , high equipment requirements, to achieve the effect of maintaining long-term operation, less dirt, and convenient flow control

Active Publication Date: 2015-03-25
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] One of the technical problems to be solved by the present invention is that in the prior art, the quenching liquid phase nozzle equipment in the multi-stage fixed-bed reactor for the production of olefins from oxygenates has high require

Method used

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  • Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds
  • Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds
  • Device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] according to figure 2 , image 3 As shown, a methanol-to-olefin reaction device, the reaction device mainly includes catalyst beds 16-21, distributors 27-31, packing layers 22-26, the uppermost layer inside the device is catalyst bed 16, catalyst bed The lower part of the layer 16 is a distributor 27, the lower part of the distributor 27 is a packing layer 22, and the lower part of the packing layer 22 is a catalyst bed 17. In this arrangement, the lowest layer inside the device is a catalyst bed 21, and an inlet is provided between each bed. The feed port and the distributor are distributed pipe ring structure.

[0028] The gas-phase reaction material 20 is divided into 5 branches and enters the device from the gas distribution device 22 in the upper part of the fixed bed area, and the liquid-phase quenching material 28 is divided into 4 branches and enters the device from the atomization device 23 in the lower part of the fixed bed area. After the inert component 24 ...

Embodiment 2

[0031] Example 1 Press figure 2 , image 3 As shown, the reaction uses ZSM-5 zeolite catalyst, the reaction temperature is 470°C, the reaction pressure is 0.06MPag, the temperature of stream 20 is 156°C, and the mass flow rate of each component is: methanol 9724 kg / h, dimethyl ether 29266 kg / h , water is 28200 kg / h, the temperature of stream 27 is 469°C, the mass flow rate of each component is: methanol 1819 kg / h, dimethyl ether 3721 kg / h, water 25841 kg / h, hydrocarbon 56753 kg / h, and the reaction pressure is 0.1 MPa(g). The four substreams of the gaseous phase reaction material 20 and the liquid phase quenching material 28 are sent to each section separately, and the streams need not be cooled or heated. The reactor can generate 450KW medium-pressure steam through the internal heat exchanger to adjust the inlet temperature of the fixed-bed catalyst in each section. Compared with Comparative Example 1, after the 16000 kg / h water is switched from the high temperature stream...

Embodiment 3

[0034] according to figure 2 , Figure 4 As shown, the reaction uses ZSM-5 zeolite catalyst, the reaction temperature is 470°C, the reaction pressure is 0.06MPag, the temperature of stream 20 is 153°C, and the mass flow rate of each component is: methanol 9724 kg / h, dimethyl ether 29266 kg / h , water 28200 kg / h, temperature of stream 27 is 469°C, mass flow rate of each component is: methanol 1819 kg / h, dimethyl ether 3721 kg / h, water 25841 kg / h, hydrocarbon 56753 kg / h, reaction pressure 0.05 MPa(g). The four substreams of the gaseous phase reaction material 20 and the liquid phase quenching material 28 are sent to each section separately, and the streams need not be cooled or heated. The reactor can generate 343KW medium-pressure steam through the internal heat exchanger to adjust the inlet temperature of each fixed-bed catalyst. Compared with [Comparative Example 1], after switching 16000 kg / h water from high-temperature stream 32 to chilled stream 32, the heating load of ...

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Abstract

The invention relates to a device for preparing olefin with oxygen compounds and application of device for preparing olefin with oxygen compounds, mainly solving the technical problems that a chilling liquid phase spray head device of a multistage fixed bed reactor for preparing olefin with oxygen compounds has high requirements and is easily blocked, the reaction temperature and the reaction air speed of the fixed bed reactor interact, and the utilization rate of the chilling liquid phase vaporization space is not high in the prior art. The device for preparing olefin with oxygen compounds mainly comprises catalyst bed layers (16-21), distributors (27-31) and packing layers (22-26), wherein the top layer in the device is the catalyst bed layer (16), the distributors are arranged below the catalyst bed layer (16), the packing layer (22) is arranged below the distributor (27), the catalyst bed layer (17) is arranged below the packing layer (22), and according to the arrangement way, the bottom layer in the device is the catalyst bed layer (21); and feeding holes are formed between bed layers, and the distributors are of ring-shaped pipe structures of distribution pipes. According to the technical scheme, the device for preparing olefin with oxygen compounds can well solve the problems, and can be used for industrial production of olefin with oxygen compounds.

Description

technical field [0001] The invention relates to a device for preparing olefins from oxygen-containing compounds and its application. Background technique [0002] Propylene is one of the basic raw materials of modern organic chemical industry. Due to the increasing demand for propylene derivatives such as polypropylene, acrylonitrile, cumene, and propylene oxide, the demand for propylene is also growing rapidly. At present, ethylene and propylene are mainly obtained through the process route using petroleum as raw material, while propylene mainly comes from the by-product of petroleum steam cracking process and catalytic cracking process. Since propylene is mainly obtained as a by-product, the output of propylene products is often limited by the output of the main product of its process. Since the demand for propylene has been higher than that of ethylene in recent years, in order to produce or increase the production of propylene, researchers have developed a variety of p...

Claims

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Application Information

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IPC IPC(8): B01J8/04B01J4/00B01J19/26C07C1/20C07C11/06
CPCB01J8/04B01J8/0492B01J2208/00752B01J2208/027C07C1/20C07C11/06
Inventor 胡帅金鑫
Owner CHINA PETROLEUM & CHEM CORP
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