Method for producing dimethyl ether from methanol by combination hydrocarbons catalytic conversion

A catalytic conversion and dimethyl ether technology, applied in chemical instruments and methods, molecular sieve catalysts, physical/chemical process catalysts, etc., can solve the problem that the amount of coke is not enough to maintain the heat balance of the process, and achieve the effect of solving the heat supply problem

Active Publication Date: 2008-01-16
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In addition, the dehydration reaction of methanol needs to be completed at a certain temperature. Although coking occurs during the reaction, the amount of coke is not enough to maintain the heat balance of the process.

Method used

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  • Method for producing dimethyl ether from methanol by combination hydrocarbons catalytic conversion
  • Method for producing dimethyl ether from methanol by combination hydrocarbons catalytic conversion

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0049] The purity of methanol in the methanol raw material is 99.5% by weight, and the hydrocarbon raw material is vacuum gas oil (VGO), and its properties are shown in Table 1. The code name of the catalyst used in this example is MTD-1 (contains 30% by weight of USY zeolite, 5% by weight of ZSM-5 zeolite, and the rest is carrier, all based on the total weight of the catalyst).

[0050] The gaseous methanol raw material enters the fluidized bed reactor and contacts with the MTD-1 catalyst. At a temperature of 280°C and a pressure (gauge pressure) of 0.1 MPa, the weight ratio of the catalyst to the methanol raw material (agent-alcohol ratio) is 2.5, and the weight hourly space velocity is 3.0h -1 Reaction under the condition of condition, reactant flow obtains coke catalyst and product flow through separation, and this product flow further separates and obtains target product dimethyl ether, and product distribution is as shown in table 2, and excessive methyl alcohol returns f...

Embodiment 2

[0055] The purity of methanol in the methanol raw material is 90.0% by weight, and the hydrocarbon raw material is VGO, and its properties are shown in Table 1. The code name of the catalyst used in the present embodiment is MTD-2 (containing 35% by weight of USY zeolite, and the balance is a carrier, all based on the total weight of the catalyst)

[0056] The liquid methanol raw material enters the fluidized bed reactor and contacts with the MTD-2 catalyst. At a temperature of 380°C and a pressure (gauge pressure) of 0.1MPa, the weight ratio of the catalyst to the methanol raw material (agent-alcohol ratio) is 40, and the weight hourly space velocity is 50h -1 Reaction under the condition of condition, reactant flow obtains coke catalyst and product flow through separation, and this product flow further separates and obtains target product dimethyl ether, and product distribution is as shown in table 2, and excessive methyl alcohol returns fluidized bed reactor; Coke catalyst ...

Embodiment 3

[0061] The purity of methanol in the methanol raw material is 95.0% by weight, and the hydrocarbon raw material is VGO, and its properties are shown in Table 1. The code name of the catalyst used in this example is MTD-3 (containing 30% by weight of USY zeolite, 5% by weight of Beta zeolite, and the balance being carrier, all based on the total weight of the catalyst).

[0062] The liquid methanol raw material enters the fluidized bed reactor and contacts with the MTD-3 catalyst. At a temperature of 150°C and a pressure (gauge pressure) of 0.1MPa, the weight ratio of the catalyst to the methanol raw material (agent-alcohol ratio) is 6, and the weight hourly space velocity is 0.1h -1 Reaction under the condition of condition, reactant flow is separated to obtain coke catalyst and product flow, and this product flow is further separated to obtain target product dimethyl ether, and product distribution is as shown in table 2, and excessive methyl alcohol returns fluidized bed reac...

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Abstract

Disclosed is a combined hydrocarbons catforming method to produce dimethyl ether from carbinol. Carbinol raw materials contact with Y zeolite catalysts and the reaction product flow is separated to get coked catalysts and target carbinol; hydrocarbon raw materials contact with Y zeolite catalysts and the reaction product flow is separated to get spent catalysts and reaction effluent and the reaction effluent is further separated to get gas and liquid products such as gasoline; all or part of the coked catalysts or spent catalysts get into a reactivator for coke-burning regeneration; the regenerated catalysts are divided into two parts, one part returns to contact with the hydrocarbon raw materials and the other part, after cooling, returns to contact with the ethanol raw materials. The method properly uses the surplus heat energy in the course of hydrocarbons catalytic conversion, solving the problem of heat energy supply in carbinol conversion, ensuring that the carbinol can be converted to dimethyl ether continuously.

Description

technical field [0001] The invention relates to a method for producing dimethyl ether from methanol, more specifically, the invention belongs to a method for producing dimethyl ether from methanol through combined catalytic conversion of hydrocarbons. Background technique [0002] There are one-step and two-step methods for the production of dimethyl ether (DME). The one-step method refers to the one-time synthesis of dimethyl ether from the raw material gas; the two-step method is to synthesize methanol from the synthesis gas, and then dehydrate to obtain dimethyl ether. [0003] The two-step method is carried out in two steps, that is, methanol is first synthesized from synthesis gas, and methanol is dehydrated under acid catalysis to produce dimethyl ether. The two-step synthesis of dimethyl ether is the main process for the production of dimethyl ether at home and abroad. This method uses refined methanol as a raw material, with few by-products of dehydration reaction, ...

Claims

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Application Information

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IPC IPC(8): C07C43/04C07C41/09B01J29/08B01J29/80
CPCY02P20/50Y02P20/584
Inventor 谢朝钢付强朱根权余少兵杨义华高永灿谢文华慕旭宏张久顺舒兴田
Owner CHINA PETROLEUM & CHEM CORP
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