CN202786065U - Dimethyl oxalate treatment and recovery system - Google Patents
Dimethyl oxalate treatment and recovery system Download PDFInfo
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- CN202786065U CN202786065U CN 201220436978 CN201220436978U CN202786065U CN 202786065 U CN202786065 U CN 202786065U CN 201220436978 CN201220436978 CN 201220436978 CN 201220436978 U CN201220436978 U CN 201220436978U CN 202786065 U CN202786065 U CN 202786065U
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- dmo
- reaction system
- recovery
- carbonylation reaction
- dimethyl oxalate
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Abstract
The utility model provides a dimethyl oxalate treatment and recovery system which comprises a carbonylation reaction system; the carbonylation reaction system comprises a DMO (dimethyl oxalate) scrubber tower, a DMO recovery tower, a recirculation cooler, a recovery tower reboiler, a DMO product tank, a scrubber tower reboiler, a DMO crude product tank, a nitrogen gas heater and a DMO recovery tank, which are communicated with one another through pipelines; the output end of the carbonylation reaction system is connected with the input end of a hydrogenation reaction system; the input end of the nitrogen gas heater is connected with the output end of the nitrogen gas heater and the output end of a nitrogen gas manifold for inputting nitrogen gas; the input port of the DMO recovery tank is communicated with all the devices of the carbonylation reaction system respectively through pipelines; and a circulating pump is arranged on a connecting pipeline between the DMO recovery tank and the DMO crude product tank. According to the utility model, the problem of crystallization of dimethyl oxalate can be solved automatically through the nitrogen gas heater, which is very convenient and does not influence running of the whole process.
Description
Technical field
The utility model relates to processing and the recovery system in the ethylene glycol production technique, specifically a kind of system that can process dimethyl oxalate crystallization and recovery.
Background technology
It is as follows that synthetic gas prepares the ethylene glycol main technique: the CO gas phase is under methyl nitrite participates in, coupling, regeneration, catalytic cycle dimethyl oxalate processed (being called for short DMO), DMO repeated hydrogenation generating glycol (being called for short EG) obtains purified ethylene glycol by rectifying separation.
The dimethyl oxalate reaction formula is
CO+2CH
3ONO-→ (COOCH
3)
2+ 2NO
It is take CO as raw material, and under strong oxidizer MN participated in, temperature of reaction was 120-140 ℃, and normal pressure carries out, and catalyzer is Pd/Al
2O
3, reactor is fixed-bed reactor.
Side reaction Formed dimethyl phthalate (DMC), its equation is:
CO?+?2CH
3ONO?—→CH
3OCOOCH
3?+?2NO
In the production, DMO, DMC, methyl alcohol, nitrogen, CO, NO, CH
3The gases such as ONO enter the DMO scrubber tower behind oxonation, DMO, DMC and methyl alcohol separate with liquid form at tower bottom, and remaining gas goes out through tower head, and then DMO separates under the DMO recovery tower.But in actual production, because steam fluctuation etc. in the operation, and pipeline adjoining pipe holding temperature is inadequate, especially at the bottom of the scrubber tower in the methanol solution DMO content greater than more than 35%, often cause under the DMO scrubber tower and recovery tower underground pipelines (comprising valve) to such an extent as to DMO crystallization device stop.At present, the normal treating method that adopts has two kinds: 1, steam is from the heating of pipeline valve outer surface, and the treatment time is long; 2, connect steam and manage temporarily, blow down to recover with steam direct heating, but DMO decomposes in hot steam, only efflux burning disposal.Though above-mentioned two kinds of methods can solve the problem of crystallization to a certain extent, but very inconvenient, had a strong impact on the normal operation of system, reduced the efficient of producing ethylene glycol.
The utility model content
The purpose of this utility model is to provide a kind of can conveniently process dimethyl oxalate processing and the recovery system that ethylene glycol is produced the crystallization of mesoxalic acid dimethyl ester.
The utility model has adopted following technical scheme: a kind of processing of dimethyl oxalate and recovery system, this system comprises the carbonylation reaction system, described carbonylation reaction system comprises the DMO scrubber tower, the DMO recovery tower, recirculation cooler, the recovery tower reboiler, DMO product groove, the scrubber tower reboiler, DMO crude product groove, rare gas element well heater and DMO accumulator tank, be interconnected through pipeline between described each device, the output terminal of described carbonylation reaction system links to each other with the hydrogenation reaction system input terminus, the input terminus of described carbonylation reaction system links to each other with the output terminal of the nitrogen header pipe that is used for input nitrogen, described nitrogen heater is located on the connection line between nitrogen header pipe and the described carbonylation reaction system, and the input aperture of DMO accumulator tank is communicated with each device in the described carbonylation reaction system respectively through pipeline; Connection line between described DMO accumulator tank and the DMO crude product groove is provided with recycle pump.
Beneficial effect: the utility model adds nitrogen heater and DMO accumulator tank in original carbonylation reaction system after, under the effect of hot nitrogen, the DMO fast liquefying is flowed in DMO crude product groove, pan tank, accumulator tank or the tower, whole system can be processed the problem of dimethyl oxalate crystallization, and is very convenient and do not affect the running of whole technique.
Description of drawings
Fig. 1 is connection diagram of the present utility model.
Among the figure: 1, nitrogen header pipe, 2, nitrogen heater, 3, the DMO scrubber tower, 4, the scrubber tower reboiler, 5, recirculation cooler, 6, the crude product groove, 7, the DMO recovery tower, 8, the recovery tower reboiler, 9, DMO product groove, 10, the DMO accumulator tank, 11, hydrogenation reaction system
12, recycle pump a, 13, recycle pump b, 14, valve a, 15, valve b.
Embodiment
Be described in further detail below in conjunction with accompanying drawing:
As shown in Figure 1, this system comprises carbonylation reaction system commonly used in the prior art, DMO described in the utility model is dimethyl oxalate and writes a Chinese character in simplified form, the input terminus of carbonylation reaction system links to each other with hydrogenation reaction system 11 with nitrogen header pipe 1 respectively, comprise DMO scrubber tower 3 in the carbonylation reaction system, scrubber tower reboiler 4, recirculation cooler 5, DMO crude product groove 6, DMO recovery tower 7, recovery tower reboiler 8 and DMO product groove 9, be interconnected with pipeline between each device, pipeline adopts aluminium section bar, be equipped with 1 to 3 valve on the connection line of each device, this system also comprises gas heater and DMO accumulator tank 10, because other rare gas elementes are not easy to extract in industrial production, so in actual production, use nitrogen heater 2, nitrogen heater 2 is located on the pipeline between nitrogen header pipe 1 and the carbonylation reaction system, DMO accumulator tank 10 through pipeline respectively with nitrogen heater 2, the carbonylation reaction system links to each other with hydrogenation reaction system 11, wherein also be provided with recycle pump a12 on DMO accumulator tank 10 and the pipeline that DMO crude product groove 6 in the carbonylation reaction system is connected, also be provided with recycle pump b13 on the connection line of DMO crude product groove 6 and recirculation cooler 5, when causing pipeline or valve blockage because of the DMO crystallization, use when at first in DMO accumulator tank 10, squeezing into certain methyl alcohol in order to dissolving, open valve a14 and the valve b15 at nitrogen heater 2 two ends, through nitrogen header pipe 1 nitrogen out enter be heated in the nitrogen heater 2 100 ~ 140 the degree, pressure-controlling is to 0.5Mpa, the DMO scrubber tower presses 3 to be 0.3Mpa, because the DMO fusing point is 54 ℃, therefore only need the operation respective valves, under the effect of hot nitrogen, the DMO fast liquefying is flowed through DMO crude product groove 6, DMO product groove 9, DMO recovery tower 7 flows in the DMO accumulator tank 10, because having methyl alcohol can dissolve rear recovery in the DMO accumulator tank 10 continues to use, not only environmental protection but also save cost, single valve or a plurality of valve crystallization can be blown down crystallization with the nitrogen after heating by the switch of controlling corresponding valve, so just can solve very easily the problem of DMO crystallization in the pipeline, reach the purpose of fast processing and recovery.
Claims (5)
1. the processing of a dimethyl oxalate and recovery system, this system comprises the carbonylation reaction system, described carbonylation reaction system comprises the DMO scrubber tower, the DMO recovery tower, recirculation cooler, the recovery tower reboiler, DMO product groove, scrubber tower reboiler and DMO crude product groove, be interconnected through pipeline between described each device, the output terminal of described carbonylation reaction system links to each other with the hydrogenation reaction system input terminus, the input terminus of described carbonylation reaction system links to each other with the output terminal of the nitrogen header pipe that is used for input nitrogen, it is characterized in that: this system also comprises nitrogen heater and DMO accumulator tank, described nitrogen heater is located on the connection line between nitrogen header pipe and the described carbonylation reaction system, and the input aperture of DMO accumulator tank is connected with each device and described nitrogen heater in the described carbonylation reaction system respectively through pipeline.
2. the processing of dimethyl oxalate according to claim 1 and recovery system, it is characterized in that: the connection line between described DMO accumulator tank and the DMO crude product groove is provided with recycle pump.
3. the processing of dimethyl oxalate according to claim 1 and recovery system is characterized in that: be equipped with valve on the connection line between described nitrogen heater and DMO accumulator tank and each device.
4. the processing of dimethyl oxalate according to claim 1 and 2 and recovery system, it is characterized in that: described nitrogen heater thermal source is 0.8 ~ 1Mpa.
5. the processing of dimethyl oxalate according to claim 1 and 2 and recovery system, it is characterized in that: the pressure of described scrubber tower and recovery tower is 0.2 ~ 0.4Mpa.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220436978 CN202786065U (en) | 2012-08-30 | 2012-08-30 | Dimethyl oxalate treatment and recovery system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220436978 CN202786065U (en) | 2012-08-30 | 2012-08-30 | Dimethyl oxalate treatment and recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202786065U true CN202786065U (en) | 2013-03-13 |
Family
ID=47813370
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220436978 Expired - Fee Related CN202786065U (en) | 2012-08-30 | 2012-08-30 | Dimethyl oxalate treatment and recovery system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202786065U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102898305A (en) * | 2012-10-30 | 2013-01-30 | 安徽淮化股份有限公司 | Dimethyl oxalate rectifying equipment |
-
2012
- 2012-08-30 CN CN 201220436978 patent/CN202786065U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102898305A (en) * | 2012-10-30 | 2013-01-30 | 安徽淮化股份有限公司 | Dimethyl oxalate rectifying equipment |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130313 Termination date: 20150830 |
|
| EXPY | Termination of patent right or utility model |