CN203842338U - Heat gradient utilization device in methanol rectification process - Google Patents
Heat gradient utilization device in methanol rectification process Download PDFInfo
- Publication number
- CN203842338U CN203842338U CN201420142146.5U CN201420142146U CN203842338U CN 203842338 U CN203842338 U CN 203842338U CN 201420142146 U CN201420142146 U CN 201420142146U CN 203842338 U CN203842338 U CN 203842338U
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- China
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- tower
- shell side
- pipeline
- tower reboiler
- reboiler
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Abstract
The utility model relates to a heat gradient utilization device in methanol rectification process. The heat gradient utilization device comprises a pressurizing rectifying tower, wherein a system crude alcohol feeding pump pipeline is sequentially connected with a middle part inlet of a pre-rectification tower through a one-level crude alcohol pre-heater tube pass and a two-level crude alcohol pre-heater tube pass; the lower section of the pre-rectification tower is connected with the bottom of the pre-rectification tower through a pre-tower reboiler tube pass; a low pressure steam pipeline and a middle pressure steam pipeline are respectively connected with a steam buffering tank; an outlet of the steam buffering tank is respectively communicated with a shell pass inlet of the upper section of a pre-tower reboiler and a shell pass inlet of a pressurizing tower reboiler; a shell pass outlet of the pressurizing tower reboiler is connected with a tube pass inlet of a pre tower rear methanol preheater through a pipeline; a shell pass outlet of the upper section of the pre tower reboiler is connected with a pipeline between the shell pass outlet of the pressurizing tower reboiler and the tube pass inlet of the pre tower rear methanol preheater; the tube pass outlet of the upper section of the pre-tower rear methanol preheater is connected with a condensing liquid tank through the shell pass of the lower section of the pre tower reboiler. The heat gradient utilization device has the advantages of less investment, simple process and low running cost.
Description
Technical field
The utility model belongs to the heat energy utilization field in methanol rectification process, is specifically related to thermal energy step use device in a kind of methanol rectification process.
Background technology
Thick alcohol heating at the bottom of needing to utilize low pressure steam to pre-tower and pressurizing tower in three-tower rectification process makes its boiling become gas to return and in tower, carry out rectifying, in three-tower rectification process, main energy consumption is the consumption of steam, at the bottom of Steam Heating is crossed tower, liquid becomes steam condensate afterwards, it is 112 DEG C that steam condensate is mixed rear temperature, after pre-tower, after methanol preheater heating pressurizing tower charging methyl alcohol, temperature is reduced to 95 DEG C and is entered condensation liquid bath, and condensate liquid is delivered to desalted water post softened water tank by condensate pump.Above-mentioned situation has two drawbacks: the one, and its heat is not fully recycled, and heat loss is larger; Also cause on the other hand desalted water post softened water tank temperature high.Meanwhile, there is the problem of three aspects: in this system: the one, and the thick alcohol feeding temperature of pre-tower is low; The 2nd, at the bottom of the tower of pre-tower reboiler, liquid methanol temperature generally between 70～75 DEG C, heats with steam; The 3rd, system evaporating cold water poor quality, causes equipment corrosion.
Utility model content
The purpose of this utility model is to overcome defect of the prior art, and a kind of a large amount of heat energy that condensing heat-exchange in methanol fractionation system produces that can make full use of are provided, reduce steam consumption, and can produce low-temperature cooling water that quality the is higher heat transferring medium as system evaporating cold, avoid causing thermal energy step use device in the methanol rectification process of equipment corrosion.
The purpose of this utility model is achieved in that and comprises compression rectification tower, the thick alcohol feed pump of system pipeline is connected with the centre inlet of pre-rectifying tower with the thick alcohol preheater of secondary tube side by the thick alcohol preheater of one-level tube side successively, at the bottom of the tower of pre-rectifying tower hypomere by pre-tower reboiler tube side and pre-rectifying tower, be connected, low-pressure steam pipeline is connected with steam buffer tank respectively with Medium Pressure Steam Pipeline, the outlet of steam buffer tank is connected with the shell side import of pre-tower reboiler epimere and the shell side import of pressurizing tower reboiler respectively, the shell side outlet of pressurizing tower reboiler is connected with the tube side import of methanol preheater after pre-tower by pipeline, pipeline between the tube side import of the shell side outlet of pre-tower reboiler epimere and methanol preheater after the shell side outlet of pressurizing tower reboiler and pre-tower is connected, after pre-tower, the tube side outlet of methanol preheater is connected with condensation liquid bath by the shell side of pre-tower reboiler hypomere, the outlet of described condensate liquid trench bottom is connected by the thick alcohol preheater of condensate pump and one-level shell side, the thick alcohol preheater of one-level shell side is connected with the shell side of moisturizing cooler by pipeline, the shell side of moisturizing cooler is connected with evaporating cold by pipeline, pipeline between described one-level thick alcohol preheater shell side and the shell side of moisturizing cooler is provided with threeway, the first end of threeway is connected with the thick alcohol preheater of one-level shell side, the second end of threeway is connected with the shell side of moisturizing cooler, the 3rd end of threeway with send pipeline outside and be connected, between the shell side of the shell side of described pre-tower reboiler epimere and pre-tower reboiler hypomere, be provided with dividing plate, described pre-tower reboiler epimere is connected with the tube side of pre-tower reboiler hypomere.The described pipeline of sending outside is connected with desalted water post.
The utility model makes it can use steam and condensed water to carry out heat exchange by changing the structure of pre-tower reboiler simultaneously, condensate liquid after heat exchange continues as the thick methyl alcohol of pre-tower charging and heats, improve pre-tower feeding temperature, reach and approach bubble point charging rectifying, above-mentioned heating can effectively reduce steam consumption; And the utility model makes full use of the Lowlevel thermal energy of condensate liquid, the condensate liquid after circulating water becomes the evaporating cold moisturizing of high-quality, has reduced the corrosion of equipment; There is small investment, technique is simple, operating cost is low, reducing the advantages such as the production cost that ensures the normal production run of system in steam loss and reduce methanol rectification process.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model.
Detailed description of the invention
As shown in Figure 1, the utility model comprises compression rectification tower 8, the thick alcohol feed pump of system pipeline 18 is connected with the centre inlet of pre-rectifying tower 10 with thick alcohol preheater 13 tube sides of secondary by thick alcohol preheater 12 tube sides of one-level successively, at the bottom of the tower of pre-rectifying tower 10 hypomeres by pre-tower reboiler 1 tube side and pre-rectifying tower 10, be connected, low-pressure steam pipeline 16 is connected with steam buffer tank 3 respectively with Medium Pressure Steam Pipeline 17, the outlet of steam buffer tank 3 is connected with the shell side import of pre-tower reboiler 1 epimere and the shell side import of pressurizing tower reboiler 2 respectively, the shell side outlet of pressurizing tower reboiler 2 is connected with the tube side import of methanol preheater 4 after pre-tower by pipeline, pipeline between the tube side import of the shell side outlet of pre-tower reboiler 1 epimere and methanol preheater 4 after the shell side outlet of pressurizing tower reboiler 2 and pre-tower is connected, after pre-tower, the tube side outlet of methanol preheater 4 is connected with condensation liquid bath 5 by the shell side of pre-tower reboiler 1 hypomere, the outlet of described condensation liquid bath 5 bottoms is connected with thick alcohol preheater 12 shell sides of one-level by condensate pump 11, thick alcohol preheater 12 shell sides of one-level are connected with the shell side of moisturizing cooler 6 by pipeline, the shell side of moisturizing cooler 6 is connected with evaporating cold 7 by pipeline, pipeline between thick alcohol preheater 12 shell sides of described one-level and the shell side of moisturizing cooler 6 is provided with threeway, the first end of threeway is connected with thick alcohol preheater 12 shell sides of one-level, the second end of threeway is connected with the shell side of moisturizing cooler 6, the 3rd end of threeway with send pipeline 9 outside and be connected, between the shell side of the shell side of described pre-tower reboiler 1 epimere and pre-tower reboiler 1 hypomere, be provided with dividing plate 14, described pre-tower reboiler 1 epimere is connected with the tube side of pre-tower reboiler 1 hypomere.The described pipeline 9 of sending outside is connected with desalted water post 15.
Operation principle of the present utility model comprises the steps: one, low-pressure steam and middle pressure steam are entered in steam buffer tank 3 and mixed by low-pressure steam pipeline 16 and Medium Pressure Steam Pipeline 17 respectively, makes mixed vapour; Two, make the mixed vapour described in step 1 enter respectively the shell side of pre-tower reboiler 1 epimere and the shell side of pressurizing tower reboiler 2 carries out heat exchange, methanol temperature after heat exchange in pre-tower reboiler 1 tube side is 70～75 DEG C, methanol temperature in pressurizing tower reboiler 2 tube sides is 125～130 DEG C, after heat exchange, mixed vapour becomes condensate liquid, the condensate temperature of the shell side outlet of pre-tower reboiler 1 epimere is 72 DEG C, and the condensate temperature of the shell side outlet of pressurizing tower reboiler 2 is 125 DEG C; Three, the condensate liquid of the shell side outlet of pre-tower reboiler 1 epimere described in step 2 is mixed in pipeline with the condensate liquid of the shell side outlet of pressurizing tower reboiler 2, mixed condensate temperature is 112 DEG C; Four, making temperature in step 3 is the tube side that the condensate liquid of 112 DEG C enters methanol preheater 4 after pre-tower, and with pre-tower after the shell side of methanol preheater 4 carry out heat exchange, the condensate temperature after heat exchange is 95 DEG C; Five, making temperature in step 4 is that the shell side that the condensate liquid of 95 DEG C enters pre-tower reboiler 1 hypomere carries out heat exchange with the methyl alcohol in pre-tower reboiler 1 tube side, and the condensate temperature after heat exchange is 82 DEG C; Six, making temperature in step 5 is that the condensate liquid of 82 DEG C enters thick alcohol preheater 12 shell sides of one-level by condensation liquid bath 5 and condensate pump 11, and with thick alcohol preheater 12 tube sides of one-level in thick heat exchange of methanol, in thick alcohol preheater 12 tube sides of one-level after heat exchange, the temperature of thick methyl alcohol is 45 DEG C; The condensate temperature in the thick alcohol preheater of one-level 12 shell side exits is 60 DEG C; Seven, making a part of temperature in step 6 is that the condensate liquid of 60 DEG C carries out heat exchange by the shell side of moisturizing cooler 6, and as high-quality, moisturizing enters in evaporating cold 7 condensate liquid after heat exchange; The temperature of the condensate liquid after described heat exchange is 20～30 DEG C; Eight, making another part temperature in step 6 is that the condensate liquid of 60 DEG C is by threeway with send pipeline 9 outside and enter desalted water post 15.In described step 2, to enter temperature in the shell side of pre-tower reboiler 1 epimere and described step 5 be that to carry out heat exchange be all for ensureing that the methanol temperature in pre-tower reboiler 1 tube side can reach 70～75 DEG C after heat exchange for shell side that the condensate liquid of 95 DEG C enters pre-tower reboiler 1 hypomere to mixed vapour.
Claims (2)
1. thermal energy step use device in a methanol rectification process, comprise compression rectification tower (8), the thick alcohol feed pump of system pipeline (18) is connected with the centre inlet of pre-rectifying tower (10) with the thick alcohol preheater of secondary (13) tube side by the thick alcohol preheater of one-level (12) tube side successively, at the bottom of the tower of pre-rectifying tower (10) hypomere by pre-tower reboiler (1) tube side and pre-rectifying tower (10), be connected, it is characterized in that: low-pressure steam pipeline (16) is connected with steam buffer tank (3) respectively with Medium Pressure Steam Pipeline (17), the outlet of steam buffer tank (3) is connected with the shell side import of pre-tower reboiler (1) epimere and the shell side import of pressurizing tower reboiler (2) respectively, the shell side outlet of pressurizing tower reboiler (2) is connected with the tube side import of methanol preheater (4) after pre-tower by pipeline, pipeline after the shell side outlet of pre-tower reboiler (1) epimere and the shell side outlet of pressurizing tower reboiler (2) and in advance tower between the tube side import of methanol preheater (4) is connected, after pre-tower, the tube side outlet of methanol preheater (4) is connected with condensation liquid bath (5) by the shell side of pre-tower reboiler (1) hypomere, the outlet of described condensation liquid bath (5) bottom is connected with the thick alcohol preheater of one-level (12) shell side by condensate pump (11), the thick alcohol preheater of one-level (12) shell side is connected with the shell side of moisturizing cooler (6) by pipeline, the shell side of moisturizing cooler (6) is connected with evaporating cold (7) by pipeline, pipeline between thick alcohol preheater (12) shell side of described one-level and the shell side of moisturizing cooler (6) is provided with threeway, the first end of threeway is connected with the thick alcohol preheater of one-level (12) shell side, the second end of threeway is connected with the shell side of moisturizing cooler (6), the 3rd end of threeway with send pipeline (9) outside and be connected, between the shell side of the shell side of described pre-tower reboiler (1) epimere and pre-tower reboiler (1) hypomere, be provided with dividing plate (14), described pre-tower reboiler (1) epimere is connected with the tube side of pre-tower reboiler (1) hypomere.
2. want thermal energy step use device in the methanol rectification process described in 1 according to right, it is characterized in that: described in send pipeline (9) outside and be connected with desalted water post (15).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420142146.5U CN203842338U (en) | 2014-03-24 | 2014-03-24 | Heat gradient utilization device in methanol rectification process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420142146.5U CN203842338U (en) | 2014-03-24 | 2014-03-24 | Heat gradient utilization device in methanol rectification process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203842338U true CN203842338U (en) | 2014-09-24 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420142146.5U Withdrawn - After Issue CN203842338U (en) | 2014-03-24 | 2014-03-24 | Heat gradient utilization device in methanol rectification process |
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| Country | Link |
|---|---|
| CN (1) | CN203842338U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861312A (en) * | 2014-03-24 | 2014-06-18 | 河南心连心化肥有限公司 | Gradient utilization device for heat energy in methanol rectifying process and utilization method of gradient utilization device |
| CN104292075A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for exchanging heat of crude alcohol in fine methanol production |
-
2014
- 2014-03-24 CN CN201420142146.5U patent/CN203842338U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103861312A (en) * | 2014-03-24 | 2014-06-18 | 河南心连心化肥有限公司 | Gradient utilization device for heat energy in methanol rectifying process and utilization method of gradient utilization device |
| CN103861312B (en) * | 2014-03-24 | 2015-10-21 | 河南心连心化肥有限公司 | In methanol rectification process, thermal energy step utilizes device and Application way thereof |
| CN104292075A (en) * | 2014-09-27 | 2015-01-21 | 安徽金禾实业股份有限公司 | Method for exchanging heat of crude alcohol in fine methanol production |
| CN104292075B (en) * | 2014-09-27 | 2016-02-03 | 安徽金禾实业股份有限公司 | The method of thick alcohol heat exchange is given in refined methanol production |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| AV01 | Patent right actively abandoned |
Granted publication date: 20140924 Effective date of abandoning: 20151021 |
|
| C25 | Abandonment of patent right or utility model to avoid double patenting |