Alkylation product separation method, alkylation reaction separation method and alkylation reaction separation device

A technology for an alkylation reaction and a separation method, which is applied in the field of the separation method and separation device of the alkylation reaction products of low-carbon olefins and alkanes, can solve problems such as inability to effectively recover and utilize, and achieves remarkable energy saving effect, easy control, and reduction of steam. The effect of the total amount

Active Publication Date: 2020-03-13
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

At least 80% of all energy consumption is used in the separation process of alkylate oil and circulating isobutane in the product. The energy loss is mainly caused by the inability to effectively recover and utilize the low-temperature heat of condensation of a large number of low-carbon hydrocarbons.

Method used

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  • Alkylation product separation method, alkylation reaction separation method and alkylation reaction separation device
  • Alkylation product separation method, alkylation reaction separation method and alkylation reaction separation device
  • Alkylation product separation method, alkylation reaction separation method and alkylation reaction separation device

Examples

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Effect test

Embodiment 1

[0049] Example 1 illustrates the effect of the separation method of the alkylation reaction product provided by the present invention.

[0050] Attached figure 1 In the reaction separation process shown, the alkylation reaction unit is the same as that of Comparative Example 1, and the alkylation reaction product obtained by the alkylation reactor is the same as that of Comparative Example 1.

[0051] Using the alkylation product separation system and method described in the present invention, the specific operating conditions are as follows: the outlet pressure of the booster pump is 3.6MPa, the outlet temperature of the cold flow heat exchanger is 76°C, the outlet temperature of the external heater is 160°C, and the vapor phase fraction 0.6, the operating pressure of the high-pressure flash tower is 3.5MPa, the vapor phase temperature at the top of the tower is 148°C, the reflux ratio is 0.6, and the liquid phase temperature at the bottom of the tower is 157°C. The vapor ph...

Embodiment 2

[0059] Example 2 illustrates the effect of the separation method for the alkylation reaction product provided by the present invention.

[0060] Attached figure 2 In the reaction separation process shown, the alkylation reaction unit is the same as that of Comparative Example 2, the reactor outlet pressure is 3.0 MPa, and the high-pressure flash pressure is 2.9 MPa, so there is no need to install a booster pump in the middle. The outlet temperature of the first heat exchanger of the cold stream is 115°C, the outlet temperature of the second heat exchanger is 135°C, the vapor phase fraction is 0.9, the vapor phase temperature at the top of the high pressure flash tower is 128°C, the reflux ratio is 0.5, and the bottom liquid The phase temperature is 133°C. The vapor phase at the top of the flash tower exchanges heat with the material at the outlet of the reactor, and the temperature drops to 120°C and condenses into a full liquid phase, and then exchanges heat with the middle...

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Abstract

The invention discloses an alkylation product separation method. According to the method, a liquid-phase alkylation product is pressurized by an optional booster pump; the pressurized liquid-phase alkylation product is introduced into a first heat exchanger, and is subjected to heat exchange with a gas-phase material from a high-pressure fractionating tower; the heat exchanged material is furtherheated to 100-180 DEG C in a second heat exchanger; the heated material enters the high-pressure fractionating tower, and is fractionated under a condition of 2.0-6.0 MPa; the gas-phase material at the top of the high-pressure fractionating tower is subjected to heat exchange with the liquid-phase alkylation product; the liquid-phase material at the bottom of the high-pressure fractionating towerenters a low-pressure fractionating tower and is fractionated under a condition of 0.2-1.0 MPa; low-carbon alkane is obtained at the top of the low-pressure fractionating tower, and an alkylation oilproduct is obtained at the bottom of the low-pressure fractionating tower; and the low-pressure fractionating tower is provided with an intermediate reboiler, and the gas-phase material at the top ofthe high-pressure fractionating tower after heat exchange of the first heat exchanger is used as a heat source of the intermediate reboiler. The method provided by the invention can improve the heat utilization efficiency and reduce the separation operation energy consumption in the alkylation process.

Description

technical field [0001] The invention relates to a mixture separation method and a separation device, more specifically, to a separation method and a separation device for alkylation reaction products of light olefins and alkanes. Background technique [0002] Alkylate is a clean, high-octane gasoline blending component. Under the action of strong acid, isoparaffins (mainly isobutane) and alkenes (C 3 ~C 5 Alkenes) react to produce alkylate. Alkylation technology can be divided into liquid acid alkylation and solid acid alkylation according to the form of catalyst. The alkylation reaction of olefins and alkanes is very complicated. The main reaction is the addition reaction of olefins and alkanes, but at the same time there are various side reactions, mainly the superposition of olefins and the cracking of macromolecules. In order to increase the concentration of the reactant isobutane and suppress the occurrence of side reactions such as superposition of olefins, it is n...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01D3/14C10G7/00C10G57/00
CPCB01D3/143C10G7/00C10G57/005Y02P20/50C10G29/205C07C7/04C07C7/005C07C2/58C07C9/16B01D3/007B01D3/06B01D3/322B01D5/0063B01D5/0075C07C2/865
Inventor 袁清毛俊义王雷黄涛赵志海李永祥胡立峰唐晓津
Owner CHINA PETROLEUM & CHEM CORP
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