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Process for producing benzene from a c5-c12 hydrocarbon mixture

A C5-C12, logistics technology, applied in the direction of metal/metal oxide/metal hydroxide catalysts, hydrocarbons, hydrocarbons, etc., can solve the problem of limited ratio control

Inactive Publication Date: 2017-05-10
SABIC GLOBAL TECH BV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] Although the method of WO 2013 / 182534 advantageously limits the amount of BTX azeotrope in the mixture obtained, the control over the ratio between benzene, toluene and xylene in the mixture obtained is limited

Method used

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  • Process for producing benzene from a c5-c12 hydrocarbon mixture
  • Process for producing benzene from a c5-c12 hydrocarbon mixture
  • Process for producing benzene from a c5-c12 hydrocarbon mixture

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0122] Two-stage hydrotreated pyrolysis gasoline having the composition shown in Table 1 was fed to a reactor containing a hydrocracking catalyst deposited on ZSM-5 with 0.03 wt% Pt, wherein the ZSM-5 The SiO2 / Al2O3 ratio was 80. Process conditions are 476°C, 200psig, H2 / HC=3, WHSV=2hr -1 . The composition of the resulting product stream is given in Table 1 below.

[0123] The benzene in the product stream is extremely pure, ie, substantially free of benzene azeotropes.

[0124] However, the amount of benzene in the product stream is no greater than in the source feed stream. Large quantities of alkylbenzenes, especially toluene and xylenes, are obtained.

[0125] Table 1

[0126] Raw materials (wt%) Product (wt%) benzene 48.11 47.75 Cyclohexane 2.87 0.01 toluene 16.03 19.22 mixed xylenes 2.83 2.85 Ethylbenzene 5.61 0.11 trimethylbenzene 0.03 0.03 Benzene purity 71.14％ 99.96％

[0127] In Table 1-4, the pu...

Embodiment 2

[0128] Embodiment 2: benzene-rich stream

[0129] A feedstock having the composition shown in Table 2 was fed into a reactor containing a hydrocracking catalyst having the same composition as the catalyst used in Example 1. The process conditions are 470°C, 200psig, H2 / HC=1, WHSV=3hr -1 . The composition of the resulting product stream is given in Table 2 below.

[0130] This example demonstrates that hydrocracking a source feedstream containing significant amounts of benzene will result in some loss of benzene, but yield reagent grade BTX from which a significant amount of reagent grade benzene can be obtained.

[0131] Table 2

[0132] Raw materials (wt%) Product (wt%) benzene 75.36 71.57 Cyclohexane 0 0.01 toluene 0 3.13 mixed xylenes 0 0.18 Ethylbenzene 0 0.25 trimethylbenzene 0 0.01 Benzene purity 78.91％ 99.83％

Embodiment 3

[0133] Embodiment 3: lean benzene stream

[0134] A feedstock having the composition shown in Table 3 was fed into a reactor containing a hydrocracking catalyst having the same composition as the catalyst used in Example 1. The process conditions are 450°C, 200psig, H2 / HC=1, WHSV=3hr -1 . The composition of the resulting product stream is given in Table 3 below.

[0135] This example describes the effect of hydrocracking a low benzene feedstock stream. It can be seen that a large amount of toluene is converted to benzene and toluene by toluene disproportionation.

[0136] table 3

[0137] Raw materials (wt%) Product (wt%) benzene 0 8.88 Cyclohexane 0 0 toluene 100 78.25 mixed xylenes 0 11.26 Ethylbenzene 0 0.01 trimethylbenzene 0 0.05 Benzene purity - 99.96％

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Abstract

The present invention relates to a process for producing benzene comprising the steps of: a) separating a source feedstream comprising C5-C12 hydrocarbons including benzene and alkylbenzenes into a first feedstream comprising a higher proportion of benzene than the source feedstream and a second feedstream comprising a lower proportion of benzene than the source feedstream and subsequently, b) contacting the first feedstream in the presence of hydrogen with a first hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size (as shown in the description) and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under first process conditions to produce a first product stream comprising benzene, wherein the first process conditions include a temperature of 425-580 DEG C, a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h-1, and c) contacting the second feedstream with hydrogen under second process conditions to produce a second product stream comprising benzene, wherein i) the second process conditions are suitable for hydrocracking and step (c) involves contacting the second feedstream in the presence of hydrogen with a second hydrocracking catalyst comprising 0.01-1 wt-% hydrogenation metal in relation to the total catalyst weight and a zeolite having a pore size of 5-8 and a silica (SiO2) to alumina (Al2O3) molar ratio of 5-200 under the second process conditions which include a temperature of 300-600 DEG C, a pressure of 300-5000 kPa gauge and a Weight Hourly Space Velocity of 0.1-15 h-1, ii) the second process conditions are suitable for toluene disproportionation and involve contacting the second feedstream with a toluene disproportionation catalyst, or iii) the second process conditions are suitable for hydrodealkylation.

Description

technical field [0001] The present invention relates to by making C containing in the presence of hydrogen 5 -C 12 A process for the production of benzene from a mixed feedstream of hydrocarbons by contacting said feedstream with a catalyst having hydrocracking activity. Background technique [0002] It has been stated in WO 02 / 44306 A1 and WO 2007 / 055488 A1 that aromatic compounds and LPG can be produced from mixed hydrocarbon feedstocks with a boiling point of 30-250°C. Therefore, a hydrocarbon feedstock with a boiling point of 30-250° C. and hydrogen are introduced into a reaction zone, wherein the hydrocarbon feedstock is hydrodealkylated and / or transalkylated into BTX-rich aromatic compounds in the presence of a catalyst and processed by adding Hydrocracking converts non-aromatic compounds rich in LPG and recovers the aromatic compounds and LPG separately by gas-liquid separation and rectification. The catalyst used in the process of WO 02 / 44306 A1 comprises platinum...

Claims

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Application Information

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IPC IPC(8): C07C4/06C07C4/18C07C6/12C07C7/04C07C15/04C10G45/00C10G45/62C10G47/18C10G65/14C10G65/18B01J29/42B01J29/44
CPCB01J29/42B01J29/44C07C4/06C07C4/18C07C6/123C07C7/04C10G45/00C10G45/62C10G47/18C10G65/14C10G65/18B01J2229/18B01J2229/42B01J2229/20C10G2400/30C07C15/04Y02P20/52B01J21/04B01J23/42B01J29/40B01J37/04C10G45/60C10G45/64C10G45/70C10G47/14B01J35/19C07C2529/44
Inventor D·费凯尔S·霍尔K·普拉沙恩特M·范埃尔赛尔S·法拉克潘纳
Owner SABIC GLOBAL TECH BV
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