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Process method and device for batch rectification of crude maleic anhydride

A process method and rectification technology, applied in the field of compound purification, can solve the problems of large interference of hot water flow in the overhead condenser of the steam system, large fluctuation of the steam flow, unfavorable stability of the steam system and the hot water system, etc. The effect of waste heat recovery, short process flow and stable steam usage

Pending Publication Date: 2020-03-27
HUIZHOU YUXIN NEW MATERIALS CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, the steam flow used in the batch distillation process fluctuates greatly, which greatly interferes with the steam system and the hot water flow of the tower top condenser, which is not conducive to the stability of the steam system and hot water system in the plant.

Method used

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  • Process method and device for batch rectification of crude maleic anhydride

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0043]Add 122670kg of crude anhydride to V-1607 to establish a total reflux reflux ratio of 8, a reflux ratio of the cut before stripping and a reflux ratio of 0.33 in the center cut. Use hot water as the heating medium, the total flow rate of the heating medium is 155556kg / h, the inlet temperature of the heating medium is 60°C, and the temperature is 85°C after being heated by E-1807 after confluence. E-1606 steam consumption in each stage is: 0kg / h for feed, 667kg / h for vacuuming, 5500kg / h for reflux in the tower, 5504kg / h for the pre-removal fraction, 7808kg / h for the center fraction, 0kg / h for breaking vacuum, and 0kg / h for preparation State 0kg / h. E-1807 steam consumption in each stage is: feeding 7900kg / h, vacuuming 7200kg / h, establishing reflux in the tower 2410kg / h, removing the front fraction 2398kg / h, center fraction 95kg / h, breaking vacuum 7850kg / h, preparing State 7850kg / h. The total amount of steam used in each stage of the whole refining tower is: feed 7900kg / h...

Embodiment 2

[0045] Add 147204kg of crude anhydride to V-1607 to establish a total reflux reflux ratio of 15, a reflux ratio of 10 for the cut before removal, and a reflux ratio of 1 for the center cut. Dibutyl phthalate (DBP) is used as the heating medium, the total flow rate of the heating medium is 1298182kg / h, the inlet temperature of the heating medium is 60°C, and the temperature is 85°C after being heated by E-1807 after confluence. E-1606 steam consumption in each stage is: feeding 0kg / h, vacuuming 800kg / h, establishing reflux in the tower 12385kg / h, removing the front fraction 9436kg / h, center fraction 28394kg / h, breaking vacuum 0kg / h, preparing State 0kg / h. E-1807 steam consumption in each stage is: feeding 28730kg / h, vacuuming 27940kg / h, establishing reflux in the tower 16330kg / h, removing the front distillate 19280kg / h, center distillate 320kg / h, breaking the vacuum 28610kg / h, preparing State 28733kg / h. The total amount of steam used in each stage of the entire refining tower...

Embodiment 3

[0047] Add 200,733 kg of crude anhydride to V-1607 to establish a total reflux reflux ratio of 8, a reflux ratio of the cut before removal, and a reflux ratio of 0.33 for the center cut. Dibutyl phthalate (DBP) is used as the heating medium, the total flow rate of the heating medium is 584182kg / h, the inlet temperature of the heating medium is 60°C, and the temperature is 85°C after being heated by E-1807 after confluence. E-1606 steam consumption in each stage is: feeding 0kg / h, vacuuming 1091kg / h, establishing reflux in the tower 9000kg / h, removing the front distillate 9007kg / h, center distillate 12777kg / h, breaking vacuum 0kg / h, preparing State 0kg / h. E-1807 steam consumption in each stage is: feeding 12910kg / h, vacuuming 11832kg / h, establishing reflux in the tower 3911kg / h, removing the front distillate 3990kg / h, center distillate 162kg / h, breaking vacuum 12944kg / h, preparing State 12912kg / h. The total amount of steam used in each stage of the whole refining tower is: fe...

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Abstract

The invention discloses a process method for batch rectification of crude maleic anhydride. The steam flow in the batch rectification process of crude maleic anhydride is stabilized. Crude anhydride is pumped into a standing tank through a pump, a reboiler is immersed in the standing tank, medium-pressure steam is used as a heat source, the gas phase of a refining tower enters a reflux tank afterbeing condensed by a tower top condenser, one part of the material in the reflux tank flows back, and the other part of the material in the reflux tank is collected out of a desorption tower or tank area. Heavy component residual anhydride in the standing tank is pumped out of the device, the overhead condenser uses hot water or other heat taking media to take heat. Except for entering the condenser, the other part of the heating medium passes through an auxiliary line and enters the heater after being converged, and the heater uses medium-pressure steam as a heat source. The flow of the heating medium is stabilized through the condenser auxiliary line regulating valve, the temperature is stabilized by heating the heated medium through steam of the heater, the effect of stabilizing the steam usage amount of the whole refining tower is achieved, the flow and the temperature of the heating medium are stable and waste heat recovery of the heating medium is facilitated.

Description

technical field [0001] The invention relates to the technical field of compound purification, in particular to a process and device for batch rectification of crude maleic anhydride. Background technique [0002] Maleic anhydride is the abbreviation of maleic anhydride, also known as maleic anhydride, which is the third largest anhydride in the world after phthalic anhydride and crude anhydride. In the past, benzene catalytic oxidation method was often used to prepare, but due to the price, now benzene method is gradually replaced by n-butane oxidation method. At present, most of the post-treatment of maleic anhydride in n-butane oxidation method adopts solvent absorption-desorption process, typical ones include Hunstman process, Conser process and ALMA process, except that ALMA uses diisobutyl hexahydrophthalate (DIBE), Both Hunstman and Conser use dibutyl phthalate (DBP) as a solvent. There have been a lot of research results on maleic anhydride oxidation process and sol...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07D307/60B01D3/00B01D3/42
CPCC07D307/60B01D3/007B01D3/42Y02P20/10Y02P20/50Y02P70/10
Inventor 夏志强黄峰黄马扶胡先念秦子轩
Owner HUIZHOU YUXIN NEW MATERIALS CO LTD
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