Method for producing aromatic hydrocarbon mixture rich in benzene, toluene and xylene by methanol conversion in fixed bed reactor

A fixed-bed reactor and methanol conversion technology, applied in the field of coal chemical industry, can solve the problems of repeated equipment construction, low efficiency, lengthy process, etc.

Active Publication Date: 2016-11-23
SHANXI FEISHI TECH +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, such a process has problems such as lengthy process, repeated equipment construction, and low efficiency.

Method used

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  • Method for producing aromatic hydrocarbon mixture rich in benzene, toluene and xylene by methanol conversion in fixed bed reactor
  • Method for producing aromatic hydrocarbon mixture rich in benzene, toluene and xylene by methanol conversion in fixed bed reactor
  • Method for producing aromatic hydrocarbon mixture rich in benzene, toluene and xylene by methanol conversion in fixed bed reactor

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0062] Refer to the accompanying drawings for the process flow diagram of methanol conversion in a fixed bed reactor to produce a BTX-rich aromatic hydrocarbon mixture in Example 1.

[0063] The inner diameter of the fixed bed reactor is 6.0m. The top is equipped with a reaction material inlet, the bottom is equipped with a reaction material outlet, and the side wall is equipped with 6 reaction material inlets. The catalyst is filled with 7 catalyst combination units. In the catalyst combination unit, methanol conversion to light olefin catalyst and light olefin aromatization catalyst Both are commercial catalysts, and the mass ratio of the two is 1.0. Among the materials entering the reactor from the top of the reactor, the mass ratio of water vapor and methanol is 5.0, and the mass ratio of circulating LPG and methanol is 1.2. Methanol mass space velocity is 0.8h -1 . The reaction pressure is 0.2 MPa.

[0064] Embodiment 1 The specific operation steps of the method for p...

Embodiment 2

[0082] All the conditions of Example 2 are the same as those of Example 1, but in the catalyst combination unit, the catalyst for converting methanol to low-carbon olefins and the catalyst for aromatizing low-carbon olefins are both commercial catalysts, and the mass ratio of the two is 2.0. Change the mass flow rate of water vapor at the top inlet of the reactor so that the mass ratio of water vapor to methanol vapor in the material entering the reactor from the top is 3.0. The mass flow rate of methanol vapor at each side wall inlet was changed accordingly to maintain the mass ratio of water to methanol entering each catalyst combination unit at 3.0. Methanol mass space velocity is 0.8h -1 , the temperature of each bed inlet material is controlled to be 400°C, and the reactor pressure is controlled to be 0.18MPa. Example 2 The loading parameters and material flow parameters of the catalyst combination unit in the fixed bed reactor are shown in Table 3.

[0083] Table 3. Th...

Embodiment 3

[0089] The inner diameter of the fixed bed reactor is 5.0m. The top is equipped with a reaction material inlet, the bottom is equipped with a reaction material outlet, and the side wall is equipped with 4 reaction material inlets. The catalyst is filled with 5 catalyst combination units. In the catalyst combination unit, methanol conversion to light olefin catalyst and light olefin aromatization catalyst Both are commercial catalysts, and the mass ratio of the two is 2.0. In the material entering the reactor from the top of the reactor, the mass ratio of water vapor and methanol is 5.0, and the mass ratio of circulating LPG and methanol is 1.5. Methanol mass space velocity is 1.0h -1 . The temperature of the inlet material of each bed is controlled to be 420°C, and the pressure of the reactor is controlled to be 0.25MPa. Example 3 The loading parameters and material flow parameters of the catalyst combination unit in the fixed bed reactor are shown in Table 5.

[0090] Tab...

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Abstract

A method for producing an aromatic mixture rich in benzene, toluene and xylene by converting methanol in a fixed-bed reactor is to pack a catalyst for converting methanol into low-carbon olefins and a low-carbon olefin aromatization catalyst in the same fixed-bed reactor , the lower layer is a low-carbon olefin aromatization catalyst, and the upper layer is a catalyst for converting methanol to a low-carbon olefin to form a catalyst combination unit; methanol steam is divided into several strands, one of which is mixed with circulating LPG and water steam, and is set at a fixed The material inlet at the top of the bed reactor enters the fixed bed reactor, and the rest of the methanol vapor enters the fixed bed reactor from the material inlet located on the side wall of the reactor to obtain a BTX-rich aromatic hydrocarbon mixture. The invention has the advantages of simple process, low cost and large-scale production.

Description

technical field [0001] The invention belongs to the technical field of coal chemical industry, and in particular relates to a method for preparing an aromatic hydrocarbon mixture rich in benzene, toluene and xylene by converting methanol in a fixed-bed reactor. Background technique [0002] Aromatics refer to a class of compounds containing benzene rings in their molecular structure. There are many types of such compounds, but the aromatics used on a large scale in industry refer to the so-called "triphenyls" including benzene, toluene and xylene, that is, BTX. So far, aromatics are mainly obtained from the reforming of naphtha in the petroleum processing process, and only a small amount of BTX products in the coal chemical industry come from the processing of crude benzene products in the coking process. [0003] Methanol can be obtained from coal conversion on a large scale and is an important cornerstone of the coal chemical industry. So far, a number of technologies for...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C15/02C07C15/04C07C15/06C07C15/08C07C1/20C07C11/02C07C2/76
Inventor 李文怀张庆庚李凯旋李晓温鹏俊张西甫范辉马国强
Owner SHANXI FEISHI TECH
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