CN219469954U - Complete treatment system for methanol rectification - Google Patents
Complete treatment system for methanol rectification Download PDFInfo
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- CN219469954U CN219469954U CN202223544827.8U CN202223544827U CN219469954U CN 219469954 U CN219469954 U CN 219469954U CN 202223544827 U CN202223544827 U CN 202223544827U CN 219469954 U CN219469954 U CN 219469954U
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Abstract
The utility model provides a complete methanol rectifying treatment system for extracting methanol in waste liquid generated in industrial-grade liquid SO2 production and improving the purpose of resource recovery.
Description
Technical Field
The utility model relates to the technical field of methanol rectification, in particular to a complete treatment system for methanol rectification.
Background
The parameters of the effluent discharged in the industrial-grade liquid SO2 production system are as follows: 30-35 wt% of methanol, 65-70 wt% of water, 0.2MPa and normal temperature, and the fact that the waste liquid contains higher content of methanol can cause environmental pollution and resource waste if the waste liquid is directly discharged outwards, and if the waste liquid can be recycled, the profit of enterprises can be improved, and the problem of pollution to the environment due to external discharge can be avoided.
Based on the above, the design provides a complete methanol rectifying treatment system.
Disclosure of Invention
The utility model aims to overcome the defects of the prior art, adapt to the actual needs, and provide a complete methanol rectifying treatment system SO as to extract methanol in waste liquid generated in industrial-grade liquid SO2 production and improve the purpose of resource recovery.
In order to achieve the purpose of the utility model, the technical scheme adopted by the utility model is as follows:
the utility model provides a complete processing system for rectifying methanol, includes raw materials pre-heater, rectifying column, first rectification condenser, second rectification condenser, raw materials pre-heater is connected with the rectifying column, and raw materials liquid gets into after the raw materials pre-heater in the rectifying column, first rectification condenser, second rectification condenser are established ties, just the light component discharge port at rectifying column top is connected first rectification condenser, the gas-liquid separator is connected to the discharge port of second rectification condenser, the water cooling circulation pipe is connected to the heat exchange tube of second rectification condenser.
The bottom of the rectifying tower is connected with a rectifying still liquid pump, a first outlet of the rectifying still liquid pump is connected with a heat exchange tube of the raw material preheater and extracts out the bottom kettle liquid of the rectifying tower to exchange heat with the raw material liquid in the raw material preheater.
And a second outlet of the rectifying still liquid pump is connected with a middle outlet of the rectifying tower to form circulation.
The rectifying tower also comprises a tower kettle circulating pump connected with the bottom of the rectifying tower, a first outlet of the tower kettle circulating pump is connected with the bottom inlet of the rectifying tower to form circulation, and a second outlet of the tower kettle circulating pump is connected with the rectifying reboiler and then connected with the inlet of the bottom of the rectifying tower to form circulation.
The rectification reboiler comprises a first rectification reboiler and a second rectification reboiler, the heat exchange pipe of the second rectification reboiler is connected with saturated steam for heat exchange, the first rectification reboiler and the second rectification reboiler are connected in series, the first rectification reboiler is connected with a tower kettle circulating pump, and the second rectification reboiler is connected with a rectification tower.
The inlet of the heat exchange tube of the first rectifying reboiler is connected with the outlet of the compressor, and the outlet of the heat exchange tube of the first rectifying reboiler is connected with the fluorine storage tank; the outlet of the fluorine storage tank is connected with the inlet of the heat exchange tube of the first rectification condenser through the heat balancer, the outlet of the heat exchange tube of the first rectification condenser is connected with the fluorine separation tank, the air outlet of the fluorine separation tank is connected with the compressor, the liquid outlet of the fluorine separation tank is connected with the fluorine circulating pump, and the outlet of the fluorine circulating pump is connected with the inlet of the heat exchange tube of the first rectification condenser to form circulation.
The bottom of the gas-liquid separator is connected with a reflux pump, the outlet of the reflux pump is divided into two branches, one branch is connected with the middle part of the rectifying tower and supplements mother liquor for the rectifying tower, and the other branch is connected with the top of the gas-liquid separator to form circulation.
The top exhaust port of the gas-liquid separator is connected with the water ring gas-liquid separation tank through a vacuum pump.
The bottom of the gas-liquid separator is connected with a methanol product pump.
The utility model has the beneficial effects that:
the system adopts a low-temperature heat pump rectification technology, the Freon working medium of the compressor is in closed cycle, in the operation process, low-pressure Freon steam is pressurized and heated by the compressor, high-pressure hot fluorine gives heat to the material liquid in a first rectification reboiler, so that the material is evaporated, and the hot fluorine is condensed into liquid; the fluorine liquid is decompressed and cooled through a throttling expansion valve, the heat of the material at the top of the tower is absorbed in a first rectifying condenser at the top of the tower to be vaporized, and then the fluorine liquid returns to a compressor to be pressurized and heated, so that the heat pump cycle is formed. The heat and cold required by evaporation and condensation of the material liquid are all provided by the heat pump system, so that the energy-saving effect is achieved.
The system can directly produce the methanol raw material which is more than or equal to 99.5 weight percent through rectification at one time, the rectification kettle liquid discharged from the tower kettle contains less than or equal to 0.1 weight percent of methanol, and meets the discharge requirement.
Drawings
Fig. 1 is a schematic diagram of the structural principle of the system.
Detailed Description
The utility model is further illustrated by the following examples in conjunction with the accompanying drawings:
example 1: a complete methanol rectification system, see fig. 1.
The device comprises a raw material preheater E101, a rectifying tower T101, a first rectifying condenser E103-1 and a second rectifying condenser E103-2, wherein the raw material preheater E101 is connected with the rectifying tower T101, raw material liquid enters the rectifying tower T101 after being preheated by the raw material preheater E101, the first rectifying condenser E103-1 and the second rectifying condenser E103-2 are connected in series, a light component discharge outlet at the top of the rectifying tower T101 is connected with the first rectifying condenser E103-1, a discharge outlet of the second rectifying condenser E103-2 is connected with a gas-liquid separator V101, and a heat exchange pipe of the second rectifying condenser E103-2 is connected with a water cooling circulation pipe for heat exchange.
The bottom of the rectifying tower T101 is connected with a rectifying still liquid pump P102, a first outlet of the rectifying still liquid pump P102 is connected with a heat exchange tube of the raw material preheater E101 and extracts out bottom liquid of the rectifying tower to exchange heat with the raw material liquid in the raw material preheater E101, and a second outlet of the rectifying still liquid pump P102 is connected with a middle outlet of the rectifying tower T101 to form circulation.
The device further comprises a tower kettle circulating pump P101 connected with the bottom of the rectifying tower T101, wherein a first outlet of the tower kettle circulating pump P101 is connected with the bottom inlet of the rectifying tower T101 to form circulation, and a second outlet of the tower kettle circulating pump P101 is connected with a rectifying reboiler and then connected with the inlet of the bottom of the rectifying tower T101 to form circulation; the rectification reboiler comprises a first rectification reboiler E102-1 and a second rectification reboiler E102-2, wherein a heat exchange pipe of the second rectification reboiler E102-2 is connected with saturated steam for heat exchange, the first rectification reboiler E102-1 and the second rectification reboiler E102-2 are connected in series, the first rectification reboiler E102-1 is connected with a tower kettle circulating pump P101, and the second rectification reboiler E102-2 is connected with a rectification tower T101.
The bottom of the gas-liquid separator is connected with a reflux pump, the outlet of the reflux pump is divided into two branches, one branch is connected with the middle part of the rectifying tower and supplements mother liquor for the rectifying tower, and the other branch is connected with the top of the gas-liquid separator to form circulation.
The top exhaust port of the gas-liquid separator V101 is connected with the water ring gas-liquid separation tank V102 through the vacuum pump P105, and the bottom of the gas-liquid separator V102 is connected with the methanol product pump P104.
In the system, the inlet of a heat exchange tube of the first rectifying reboiler E102-1 is connected with the outlet of the compressor C201, and the outlet of the heat exchange tube of the first rectifying reboiler E102-1 is connected with the fluorine storage tank V201; the outlet of the fluorine storage tank V201 is connected with the inlet of a heat exchange tube of the first rectifying condenser E103-1 through a heat balancer E201, the outlet of the heat exchange tube of the first rectifying condenser E103-1 is connected with a fluorine separation tank V202, the air outlet of the fluorine separation tank V202 is connected with the inlet of the compressor C201, the liquid outlet of the fluorine separation tank V202 is connected with a fluorine circulating pump P201, and the outlet of the fluorine circulating pump P201 is connected with the inlet of the heat exchange tube of the first rectifying condenser E103-1 to form circulation.
In operation, dilute methanol raw material liquid pumped from raw materials is moved downwards to form kettle liquid after the raw materials are pre-and recombinant, the kettle liquid is gasified by a first rectifying reboiler and a second rectifying reboiler and then enters a tower again, light components enter a first rectifying condenser and a second rectifying condenser to be condensed and then flow back to a gas-liquid separator, in the process, liquid is subjected to mass transfer and heat transfer in the rectifying tower, qualified methanol is obtained from the top of the rectifying tower, and then the qualified methanol is separated by the gas-liquid separator and is pumped out of the boundary by a methanol product pump to form a methanol product.
Circulating from the bottom of the rectifying tower to the kettle liquid containing a trace of methanol by a rectifying kettle liquid pump to improve the rectifying efficiency, and finally pumping the kettle liquid after multiple times of circulation out of the tank liquid through the rectifying kettle liquid pump to treat wastewater; and the kettle liquid with higher temperature is upwards conveyed to a first rectifying reboiler through a tower kettle circulating pump for mass transfer and heat exchange, is heated and gasified by high-temperature Freon compressed by a compressor, and is conveyed to the rectifying tower again.
In the process, the freon in the fluorine storage tank is throttled after heat is recovered in the heat balancer, then enters the first rectification condenser, then enters the fluorine separation tank, the gasified freon after entering the fluorine separation tank is heated and boosted after entering the compressor for compression, then enters the first rectification reboiler for heat exchange, the pressurized freon is liquefied in the first rectification reboiler and then returns to the fluorine storage tank, and the liquid in the fluorine separation tank is sent into the first rectification condenser through the fluorine circulation pump to condense the methanol for circulation.
The embodiments of the present utility model are disclosed as preferred embodiments, but not limited thereto, and those skilled in the art will readily appreciate from the foregoing description that various modifications and variations can be made without departing from the spirit of the present utility model.
Claims (9)
1. A complete methanol rectifying treatment system is characterized in that: the device comprises a raw material preheater, a rectifying tower, a first rectifying condenser and a second rectifying condenser, wherein the raw material preheater is connected with the rectifying tower, raw material liquid enters the rectifying tower after being preheated by the raw material preheater, the first rectifying condenser and the second rectifying condenser are connected in series, a light component discharge outlet at the top of the rectifying tower is connected with the first rectifying condenser, a discharge outlet of the second rectifying condenser is connected with a gas-liquid separator, and a heat exchange tube of the second rectifying condenser is connected with a water cooling circulation tube.
2. The methanol rectification plant of claim 1, wherein: the bottom of the rectifying tower is connected with a rectifying still liquid pump, a first outlet of the rectifying still liquid pump is connected with a heat exchange tube of the raw material preheater and extracts out the bottom kettle liquid of the rectifying tower to exchange heat with the raw material liquid in the raw material preheater.
3. The methanol rectification plant of claim 2, wherein: and a second outlet of the rectifying still liquid pump is connected with a middle outlet of the rectifying tower to form circulation.
4. The methanol rectification plant of claim 2, wherein: the rectifying tower also comprises a tower kettle circulating pump connected with the bottom of the rectifying tower, a first outlet of the tower kettle circulating pump is connected with the bottom inlet of the rectifying tower to form circulation, and a second outlet of the tower kettle circulating pump is connected with the rectifying reboiler and then connected with the inlet of the bottom of the rectifying tower to form circulation.
5. The methanol rectifying unit processing system as set forth in claim 4, wherein: the rectification reboiler comprises a first rectification reboiler and a second rectification reboiler, the heat exchange pipe of the second rectification reboiler is connected with saturated steam for heat exchange, the first rectification reboiler and the second rectification reboiler are connected in series, the first rectification reboiler is connected with a tower kettle circulating pump, and the second rectification reboiler is connected with a rectification tower.
6. The methanol rectifying unit processing system as set forth in claim 5, wherein: the inlet of the heat exchange tube of the first rectifying reboiler is connected with the outlet of the compressor, and the outlet of the heat exchange tube of the first rectifying reboiler is connected with the fluorine storage tank; the outlet of the fluorine storage tank is connected with the inlet of the heat exchange tube of the first rectification condenser through the heat balancer, the outlet of the heat exchange tube of the first rectification condenser is connected with the fluorine separation tank, the air outlet of the fluorine separation tank is connected with the compressor, the liquid outlet of the fluorine separation tank is connected with the fluorine circulating pump, and the outlet of the fluorine circulating pump is connected with the inlet of the heat exchange tube of the first rectification condenser to form circulation.
7. The methanol rectifying unit processing system as set forth in claim 6, wherein: the bottom of the gas-liquid separator is connected with a reflux pump, the outlet of the reflux pump is divided into two branches, one branch is connected with the middle part of the rectifying tower and supplements mother liquor for the rectifying tower, and the other branch is connected with the top of the gas-liquid separator to form circulation.
8. The methanol rectifying unit processing system of claim 7, wherein: the top exhaust port of the gas-liquid separator is connected with the water ring gas-liquid separation tank through a vacuum pump.
9. The methanol rectifying unit processing system of claim 8, wherein: the bottom of the gas-liquid separator is connected with a methanol product pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223544827.8U CN219469954U (en) | 2022-12-29 | 2022-12-29 | Complete treatment system for methanol rectification |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223544827.8U CN219469954U (en) | 2022-12-29 | 2022-12-29 | Complete treatment system for methanol rectification |
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| Publication Number | Publication Date |
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| CN219469954U true CN219469954U (en) | 2023-08-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202223544827.8U Active CN219469954U (en) | 2022-12-29 | 2022-12-29 | Complete treatment system for methanol rectification |
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| CN (1) | CN219469954U (en) |
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- 2022-12-29 CN CN202223544827.8U patent/CN219469954U/en active Active
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