CN204932908U - A kind of sequence of constant boiling and rectification device for maleic anhydride production - Google Patents
A kind of sequence of constant boiling and rectification device for maleic anhydride production Download PDFInfo
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- CN204932908U CN204932908U CN201520669202.5U CN201520669202U CN204932908U CN 204932908 U CN204932908 U CN 204932908U CN 201520669202 U CN201520669202 U CN 201520669202U CN 204932908 U CN204932908 U CN 204932908U
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Abstract
The utility model discloses a kind of sequence of constant boiling and rectification device for maleic anhydride production, comprise feed line, dimethylbenzene groove and azeotropic tower, feed line is connected with concentration heater and gas-liquid separator in turn, the gaseous phase outlet of gas-liquid separator is connected with concentrated condenser, outlet at bottom is connected with azeotropic tower, the gas vent of azeotropic top of tower is connected with dehydration condenser, quantizer, water sealed tank, dimethylbenzene groove and distillation still in turn, the gaseous phase outlet of distillation still is connected with the steam inlet of azeotropic tower bottom, and the liquid-phase outlet of azeotropic tower bottom is connected with thick acid anhydride tank.The utility model not only increases the speed of dehydration, completely avoid the generation of side reaction, the steady quality of product after concentrated, the use amount of dehydrating agent is little, and effect control production cost, the recovery utilization rate of dehydrating agent is higher, effectively raises refining ability, bring good economic benefit to enterprise, be easy to promote the use of.
Description
Technical field
The utility model belongs to chemical mechanical equipment technical field, is specifically related to a kind of sequence of constant boiling and rectification device for maleic anhydride production.
Background technology
Cis-butenedioic anhydride is a kind of important Organic Chemicals, obtains use widely in fields such as plastics industry, paper industry, synthetic resin industry, coatings industry, pesticide industry, medical industries.At present, the production of cis-butenedioic anhydride is for haul with benzene and air, catalyst is adopted to generate cis-butenedioic anhydride material gas through fixing oxidation bed oxidation, the cis-butenedioic anhydride material gas generated is after fractional distilling tube condensation, gas enters into the suitable acid solution that absorption tower is concentration 40% by soft water absorption, the suitable acid solution of 40% enters into sequence of constant boiling and rectification section and utilizes dehydrating agent to slough water in Free water and molecule, dehydrating agent is ortho-xylene, dimethylbenzene recycles, thick acid anhydride after dehydration is driven in continuous azeotropic tower and carries out rectifying from thick acid anhydride tank, can obtain the cis-butenedioic anhydride of finished product.Concentration is that the suitable acid solution of 40% is in the process of sequence of constant boiling and rectification, its equipment adopted is azeotropic tower and dimethylbenzene heater mainly, dehydrating agent dimethylbenzene is entered from the bottom of azeotropic tower after heater heating, and the suitable acid solution of 40% enters from the top of azeotropic tower, react with dehydrating agent in azeotropic tower, thus the moisture sloughed in the suitable acid solution of 40%, the suitable acid solution of 60% is obtained after reaction, the suitable acid solution of 60% is discharged from the bottom of azeotropic tower, dimethylbenzene after dehydration and the mixture of steam are then discharged from the neck of azeotropic tower, above-mentioned rectifier unit finds that in the production and application process of reality dimethylbenzene adopts in the process of heater heating, enter the non-uniform temperature of the dimethylbenzene in azeotropic tower, the separation completely realizing gas-liquid that can not be higher in azeotropic tower, concentrated cis-butenedioic anhydride solution quality is unstable, well can not remove the moisture in raw material, if fruit will realize good separating effect, improve the speed of dehydration, not only just need to consume a large amount of steam, and due to the fluctuating range of temperature large, the moisture contained in raw material can form a certain amount of sour regurgitation accessory substance in the process of rectifying, not only wasted a large amount of energy but also the serious yield that have impact on product, impact is brought to the economic benefit of enterprise, simultaneously, in the process of rectifying, in azeotropic tower, the use amount of dehydrating agent is larger, virtually add production cost, and directly put from the mixture that azeotropic tower top is discharged, while increase environmental pollution, also can the life cycle of shortening equipment greatly, easy etching apparatus, and then reduce production capacity.Therefore, developing that a kind of reasonable in design, dewatering speed is fast, constant product quality, product yield are high, dehydrating agent recovery utilization rate is high, side reaction is few, effectively can reduce the sequence of constant boiling and rectification device for maleic anhydride production of production cost is desirability.
Summary of the invention
The purpose of this utility model be to provide a kind of reasonable in design, dewatering speed fast, constant product quality, product yield are high, dehydrating agent recovery utilization rate is high, side reaction is few, effectively can reduce the sequence of constant boiling and rectification device for maleic anhydride production of production cost.
The purpose of this utility model realizes like this, comprise feed line, dimethylbenzene groove and azeotropic tower, feed line is connected with the import of concentration heater, the outlet of concentration heater is connected with gas-liquid separator, the gaseous phase outlet at gas-liquid separator top is connected with concentrated condenser, outlet at bottom is connected with azeotropic tower, the condensate outlet of concentrated condenser is connected with dilture acid tank, the gas vent of azeotropic top of tower is connected with dehydration condenser, the condensate outlet of dehydration condenser is connected with quantizer, the dimethylbenzene outlet of quantizer is connected by the refluxing opening of pipeline with azeotropic tower, the liquid outlet of quantizer is connected with water sealed tank, the dimethylbenzene outlet of water sealed tank is connected with dimethylbenzene groove, the outlet of dimethylbenzene groove is connected with distillation still by dimethylbenzene pump and pipeline, the gaseous phase outlet of distillation still is connected with the steam inlet of azeotropic tower bottom, the liquid-phase outlet of azeotropic tower bottom is connected with thick acid anhydride tank.
The distillation still of the utility model by arranging, the speed not only heated is fast, and effectively can ensure the temperature constant of dehydrating agent in tower, thus improve the speed of dehydration, completely avoid the generation of side reaction, the steady quality of product after concentrated, and effectively reduce the use amount of dehydrating agent, improve the yield of product greatly, compare traditional rectifier unit, the yield of product improves about 20%
,simultaneously, dehydrating agent in the exhaust-gas mixture of generation can also be carried out recovery cycling and reutilization, not only the recovery utilization rate of dehydrating agent is higher, and effectively control production cost, decrease the use amount of dehydrating agent, effectively raise refining ability, bring good economic benefit to enterprise, be easy to promote the use of.
Accompanying drawing explanation
Fig. 1 is overall structure schematic diagram of the present utility model;
In figure: 1-distillation still, 2-cuts a tank, the thick acid anhydride tank of 3-, 4-feed line, 5-sour water pump, 6-inlet valve, 7-azeotropic tower, 8-concentration heater, 9-gas-liquid separator, 10-dilture acid tank, 11-concentrates condenser, 12-return duct, 13-dewaters condenser, 14-temperature monitoring, 15-quantizer, 16-water sealed tank, 17-type washing trough, 18-dimethylbenzene groove, 19-dimethylbenzene pump, 20-waste effluent flume, 21-reboiler.
Detailed description of the invention
Be further described the utility model below in conjunction with accompanying drawing, but limited the utility model never in any form, any change done based on the utility model training centre or improvement, all belong to protection domain of the present utility model.
As shown in Figure 1, the utility model comprises feed line 4, dimethylbenzene groove 18 and azeotropic tower 7, feed line 4 is connected with the import of concentration heater 8, the outlet of concentration heater 8 is connected with gas-liquid separator 9, the gaseous phase outlet at gas-liquid separator 9 top is connected with concentrated condenser 11, outlet at bottom is connected with azeotropic tower 7, the condensate outlet of concentrated condenser 11 is connected with dilture acid tank 10, the gas vent at azeotropic tower 7 top is connected with dehydration condenser 13, the condensate outlet of dehydration condenser 13 is connected with quantizer 15, the dimethylbenzene outlet of quantizer 15 is connected by the refluxing opening of pipeline with azeotropic tower 7, the liquid outlet of quantizer 15 is connected with water sealed tank 16, the dimethylbenzene outlet of water sealed tank 16 is connected with dimethylbenzene groove 18, the outlet of dimethylbenzene groove 18 is connected with distillation still 1 by dimethylbenzene pump 19 and pipeline, the gaseous phase outlet of distillation still 1 is connected with the steam inlet bottom azeotropic tower 7, liquid-phase outlet bottom azeotropic tower 7 is connected with thick acid anhydride tank 3.
Further, the water outlet of described water sealed tank 16 is connected with type washing trough 17, the delivery port of described type washing trough 17 is connected with the washings import of azeotropic tower 7 by pipeline, blow-off pipe bottom described distillation still 1 is connected with reboiler 21, the exit of described reboiler 21 is provided with waste effluent flume 20, described blow-off pipe is also provided with blowoff valve, is can complete cleaning to azeotropic tower 7 to pass through the moisture after deviating from economize energy while
Further, liquid-phase outlet bottom described azeotropic tower 7 and the main line between thick acid anhydride tank 3 are also provided with branch line, described branch line is connected with and cuts a tank 2, described main pipe rail and branch line are all provided with by-pass valve control, be the quality in order to concentrated rear cis-butenedioic anhydride acid solution better can be ensured, thus realize the collection to the de-front-end volatiles after dehydration and de-tails.
Further, described feed line 4 is provided with sour water pump 5 and inlet valve 6, the tower body of described azeotropic tower 7 being provided with thermocouple thermometer and temperature detector 14, is to better control quantity of steam and sour water amount, ensures carrying out smoothly of dehydration.
Further, the delivery port of described water sealed tank 16 is also connected with dilture acid tank 10 by return duct 12.
Further, at least 2 heaters are provided with in described distillation still 1, the housing of described distillation still 1 is outside equipped with chuck, the outer surface of described insulation jacket scribbles insulating moulding coating layer, is better to be incubated distillation still to realize, and ensures the homogeneous temperature of dimethylbenzene in still, the time of heating can also be reduced simultaneously, reach energy-conservation object, the insulating moulding coating layer of setting can also further reduce scattering and disappearing of heat, the workman of operation of also can not burning because of heating.
Further, the tower reactor section outer surface of described azeotropic tower 7 is provided with heating semicanal, is the homogeneous temperature in order to ensure tower reactor at any time, to improve the speed of dehydration.
Further, 2 pieces of float valve trays and 14 pieces of sieve trays are disposed with from top to bottom in the tower body of described azeotropic tower 7, arranging float valve tray is in order to the flux for controlling gas, thus save the loss of steam, sieve tray is set and can reduces pressure reduction, improve the ability of producing, effective guarantee send sour ability.
The course of work of the present utility model is: first 40% cis-butenedioic anhydride sour water enters concentration heater 8, 40% cis-butenedioic anhydride sour water is heated with low-pressure steam, gas-liquid separator 9 is entered after 40% cis-butenedioic anhydride sour water being heated to about 80 DEG C under pressure under vacuo, concentrated condenser 11 is entered by the gas phase after gas-liquid separator 9 is separated, flow in dilture acid tank 10 with the condensed pickle of recirculated cooling water, azeotropic tower 7 is entered into from gas-liquid separator 9 60% concentrated acid water out, in the process that 40% cis-butenedioic anhydride sour water is concentrated, regulate by the amount controlling low-pressure steam in the outlet temperature of concentration heater 8, the 60% concentrated acid water sour water amount entered in azeotropic tower 7 is controlled by temperature monitoring, after the liquid level of distillation still 1 arrives the upper limit, concentration heater 8 stops heating, then vacuum is stopped, concentration heater 8 charging is stopped after 20 minutes, distillation still 1 stops heating, now, enter the xylene steam generation dehydration that 60% concentrated acid water in azeotropic tower 7 and distillation still 1 pass into, reacted water and xylene mixture steam from azeotropic tower 7 top, after the condensation of dehydration condenser 13, the mixture of dimethylbenzene and water carries out Liquid liquid Separation in quantizer 15, the dimethylbenzene on upper strata is as overhead reflux liquid, lower layer of water is after water sealed tank 16 is separated again, water supplements fresh water (FW) to dilture acid tank 10 as absorption tower by return line flow, and the dimethylbenzene that water sealed tank 16 branches away flows in dimethylbenzene groove 18, when needs clean azeotropic tower 7, the deionized water reclaimed in type washing trough 17 is sent into azeotropic tower 7 by washing water pump, when the heat exchanging pipe of deionized water submergence distillation still 1, tower top valve turns to from distillation and washes tower-like state, make washings at reflux in tower, after cleaning, open the blowoff valve bottom distillation still 1, sewage is sent into reboiler 21 to cool rear discharge and enter in waste effluent flume.
Claims (8)
1. the sequence of constant boiling and rectification device for maleic anhydride production, comprise feed line (4), dimethylbenzene groove (18) and azeotropic tower (7), it is characterized in that: described feed line (4) is connected with the import of concentration heater (8), the outlet of concentration heater (8) is connected with gas-liquid separator (9), the gaseous phase outlet at gas-liquid separator (9) top is connected with concentrated condenser (11), outlet at bottom is connected with azeotropic tower (7), the condensate outlet of concentrated condenser (11) is connected with dilture acid tank (10), the gas vent at azeotropic tower (7) top is connected with dehydration condenser (13), the condensate outlet of dehydration condenser (13) is connected with quantizer (15), the dimethylbenzene outlet of quantizer (15) is connected by the refluxing opening of pipeline with azeotropic tower (7), the liquid outlet of quantizer (15) is connected with water sealed tank (16), the dimethylbenzene outlet of water sealed tank (16) is connected with dimethylbenzene groove (18), the outlet of dimethylbenzene groove (18) is connected with distillation still (1) by dimethylbenzene pump (19) and pipeline, the gaseous phase outlet of distillation still (1) is connected with the steam inlet of azeotropic tower (7) bottom, the liquid-phase outlet of azeotropic tower (7) bottom is connected with thick acid anhydride tank (3).
2. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, it is characterized in that: the water outlet of described water sealed tank (16) is connected with type washing trough (17), the delivery port of type washing trough (17) is connected by the washings import of pipeline with azeotropic tower (7), the blow-off pipe of distillation still (1) bottom is connected with reboiler (21), the exit of reboiler (21) is provided with waste effluent flume (20), and blow-off pipe is also provided with blowoff valve.
3. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, it is characterized in that: the main line between the liquid-phase outlet of azeotropic tower (7) bottom and thick acid anhydride tank (3) is also provided with branch line, branch line is connected with and cuts a tank (2), main pipe rail and branch line are all provided with by-pass valve control.
4. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, it is characterized in that: feed line (4) is provided with sour water pump (5) and inlet valve (6), the tower body of azeotropic tower (7) is provided with thermocouple thermometer and temperature detector (14).
5. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, is characterized in that: the delivery port of water sealed tank (16) is also connected with dilture acid tank (10) by return duct (12).
6. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, it is characterized in that: distillation still is provided with at least 2 heaters in (1), the housing of distillation still (1) is outside equipped with chuck, and the outer surface of insulation jacket scribbles insulating moulding coating layer.
7. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, is characterized in that: the tower reactor section outer surface of azeotropic tower (7) is provided with heating semicanal.
8. a kind of sequence of constant boiling and rectification device for maleic anhydride production according to claim 1, is characterized in that: be disposed with 2 pieces of float valve trays and 14 pieces of sieve trays in the tower body of azeotropic tower (7) from top to bottom.
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| CN201520669202.5U CN204932908U (en) | 2015-09-01 | 2015-09-01 | A kind of sequence of constant boiling and rectification device for maleic anhydride production |
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| CN201520669202.5U CN204932908U (en) | 2015-09-01 | 2015-09-01 | A kind of sequence of constant boiling and rectification device for maleic anhydride production |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112110796A (en) * | 2020-09-16 | 2020-12-22 | 内蒙古格林特制药有限责任公司 | Resorcinol refining method and concentration distillation equipment |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112110796A (en) * | 2020-09-16 | 2020-12-22 | 内蒙古格林特制药有限责任公司 | Resorcinol refining method and concentration distillation equipment |
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