CN219072104U - Methanol tail liquid treatment system for glycine production - Google Patents
Methanol tail liquid treatment system for glycine production Download PDFInfo
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- CN219072104U CN219072104U CN202223466832.1U CN202223466832U CN219072104U CN 219072104 U CN219072104 U CN 219072104U CN 202223466832 U CN202223466832 U CN 202223466832U CN 219072104 U CN219072104 U CN 219072104U
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- methyl alcohol
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The utility model belongs to the field of methanol tail liquid treatment systems, and particularly relates to a methanol tail liquid treatment system for glycine production, which comprises a methanol recovery tank, a methanol rectifying tower, a reboiler, an ammonium chloride purification unit and a methanol purification unit, wherein the methanol purification unit further comprises a methanol splitting device, the methanol splitting device is positioned between a condenser and a reflux tank, the methanol splitting device comprises a methanol buffer tank and a plurality of methanol splitting tanks connected with the methanol buffer tank in parallel, a feed inlet of the methanol buffer tank is connected with the condenser, and a discharge outlet of the methanol splitting tank is connected with the methanol reflux tank. According to the utility model, the methanol diversion device is arranged, the methanol is collected by the methanol diversion tanks and circularly flows into the methanol reflux tank for detection, so that the methanol tail liquid treatment system can continuously work, and the methanol tail liquid treatment efficiency is improved.
Description
Technical Field
The utility model belongs to the field of methanol tail liquid treatment systems, and particularly relates to a methanol tail liquid treatment system for glycine production.
Background
In the production process of the glycine, a large amount of methanol is required to be used for extracting the glycine, and the methanol tail liquid recovered after centrifugation contains more ammonium chloride impurities, so that the purity of the methanol is influenced, and therefore, the methanol tail liquid is required to be purified.
In the prior art, units consisting of a condenser, a reflux tank and a rectifying tower are generally adopted for circulating rectification purification, but in the circulating rectification process, the concentration of the early methanol is high, the concentration of the late methanol is low, multiple times of circulation are needed, and the whole methanol tail liquid treatment system cannot continuously work during the circulating rectification, so that the methanol tail liquid treatment efficiency is poor.
Disclosure of Invention
The utility model aims to solve the problems in the prior art, and provides a methanol tail liquid treatment system for glycine production.
The utility model adopts the specific technical scheme that:
the utility model provides a glycine production is with methyl alcohol tail liquid processing system, includes methyl alcohol recovery tank, methyl alcohol rectifying column, reboiler, ammonium chloride purification unit and methyl alcohol purification unit, the methyl alcohol recovery tank is connected with the feed inlet of methyl alcohol rectifying column, the feed inlet and the discharge gate of reboiler are connected with the methyl alcohol rectifying column respectively, and the raffinate discharge gate of methyl alcohol rectifying column is connected with ammonium chloride purification unit, the steam discharge gate of methyl alcohol rectifying column is connected with the methyl alcohol purification unit, the ammonium chloride purification unit includes the knockout drum and the chloroacetic acid crystallization kettle who is connected with the knockout drum, the knockout drum is connected with the raffinate discharge gate of methyl alcohol rectifying column, the methyl alcohol purification unit includes condenser, reflux drum and the methyl alcohol holding vessel that connects gradually, the condenser is connected with the gas discharge gate of methyl alcohol rectifying column, the reflux drum's back flow is connected with the methyl alcohol rectifying column, the methyl alcohol purification unit still includes methyl alcohol diverging device, the condenser is connected with the reflux drum with the help of methyl alcohol diverging device, methyl alcohol diverging device includes methyl alcohol buffer tank and a plurality of methyl alcohol diverging tanks parallelly connected with the methyl alcohol buffer tank, the feed inlet and the condenser is connected with the reflux drum.
The methanol diversion device further comprises a ball float valve, and the ball float valve is positioned between the methanol cache tank and the methanol diversion tank.
The feed inlet department of methyl alcohol reflux drum is equipped with methyl alcohol feed pump, and the discharge gate department of methyl alcohol reflux drum is equipped with the methyl alcohol extraction pump.
An ammonium chloride tail liquid buffer tank is arranged between the methanol rectifying tower and the separating tank.
The device is characterized in that an auxiliary electric heating tank is further arranged between the ammonium chloride tail liquid buffer tank and the separating tank, the auxiliary electric heating tank is connected with the ammonium chloride buffer tank by means of a heat exchanger, the heat exchanger comprises a first heat exchanger and a second heat exchanger which are mutually connected, the first heat exchanger is connected with a discharge hole of the ammonium chloride tail liquid buffer tank, and the second heat exchanger is connected with a feed hole of the separating tank by means of an auxiliary electric heating pipe.
And a circulating pump is arranged between the separating tank and the second heat exchanger.
The separation tank and the second heat exchanger are also provided with a secondary evaporation device, the secondary evaporation device comprises a demister and a compressor, the air inlet end of the demister is connected with the separation tank, and the air outlet end of the demister is connected with the second heat exchanger by means of the compressor.
The beneficial effects of the utility model are as follows:
1. according to the utility model, the methanol is collected by the methanol diversion device through the methanol diversion tanks and circularly flows into the methanol reflux tank for detection, so that the whole methanol purification process is changed from intermittent operation to circular continuous operation, and the methanol tail liquid treatment efficiency is improved.
2. According to the utility model, the two heat exchangers are matched with the secondary evaporation device, the secondary steam discharged from the separation tank is used as the heat source of the second heat exchanger, and the secondary steam passes through the second heat exchanger to form high-temperature condensed water as the heat source of the first heat exchanger, so that the thermal cycle is realized, the use of an auxiliary electric heating tank is reduced, and the energy consumption is reduced.
Drawings
Fig. 1 is a schematic diagram of a system structure according to the present utility model.
Detailed Description
The utility model provides a glycine production is with methyl alcohol tail liquid processing system, includes methyl alcohol recovery tank, methyl alcohol rectifying column, reboiler, ammonium chloride purification unit and methyl alcohol purification unit, the methyl alcohol recovery tank is connected with the feed inlet of methyl alcohol rectifying column, the feed inlet and the discharge gate of reboiler are connected with the methyl alcohol rectifying column respectively, and the raffinate discharge gate of methyl alcohol rectifying column is connected with ammonium chloride purification unit, the steam discharge gate of methyl alcohol rectifying column is connected with the methyl alcohol purification unit, the ammonium chloride purification unit includes the knockout drum and the chloroacetic acid crystallization kettle who is connected with the knockout drum, the knockout drum is connected with the raffinate discharge gate of methyl alcohol rectifying column, the methyl alcohol purification unit includes condenser, reflux drum and the methyl alcohol holding vessel that connects gradually, the condenser is connected with the gas discharge gate of methyl alcohol rectifying column, the reflux drum's back flow is connected with the methyl alcohol rectifying column, the methyl alcohol purification unit still includes methyl alcohol diverging device, the condenser is connected with the reflux drum with the help of methyl alcohol diverging device, methyl alcohol diverging device includes methyl alcohol buffer tank and a plurality of methyl alcohol diverging tanks parallelly connected with the methyl alcohol buffer tank, the feed inlet and the condenser is connected with the reflux drum.
In the existing methanol tail liquid treatment system, after the methanol tail liquid is rectified by a methanol rectifying tower, the ammonium chloride residual liquid flows into a separating tank for flash evaporation, the ammonium chloride concentrated solution obtained by flash evaporation flows into a chloroacetic acid crystallizing kettle for cooling and crystallizing to obtain solid ammonium chloride, methanol steam flows into a condenser for liquefying, the methanol with qualified purity flows into a methanol storage tank, and the methanol with unqualified purity flows into the methanol rectifying tower through a reflux pipe of a reflux tank for repeated purification, but in the process of methanol purification, the methanol with high purity at the front and low purity at the back is mixed with the methanol with high purity, so that the purity of the methanol mixed liquid does not reach the standard, qualified high-purity methanol is polluted, continuous reflux purification is needed, and therefore, the methanol tail liquid of the next batch is purified after the methanol tail liquid of each batch is purified to be qualified, and the working efficiency is low.
As shown in figure 1, a methanol buffer tank and three methanol diversion tanks are arranged in the utility model, methanol steam is liquefied by a condenser and flows into the methanol buffer tank to be collected, then flows into the three methanol diversion tanks respectively from the methanol buffer tank, methanol in the methanol diversion tank 1# can flow into a reflux tank to be detected, methanol with purity of over 93% flows into a methanol storage tank, unqualified methanol can flow into a methanol rectifying tower again to be rectified and purified through a reflux pipe of the reflux tank, when unqualified methanol flows into the rectifying tower to be rectified and purified again, methanol in the methanol diversion tank 2# can flow into the reflux tank to be detected, qualified methanol flows into the methanol storage tank, unqualified methanol flows into the methanol rectifying tower, and similarly, methanol in the methanol diversion tank 3# is repeatedly subjected to the operation, and in the process of detecting and collecting the methanol diversion tank 2# and the methanol diversion tank 3#, the reflux methanol can be rectified again and flows into the methanol diversion tank 1#, so that the mixture of lower purity and the methanol with high purity is avoided, and simultaneously when the unqualified methanol flows into the rectifying tank again to be rectified, the methanol can flow into the reflux tank to be detected, and the methanol is continuously purified, and the work is continuously and intermittently circulated from the collecting tank to be purified.
Furthermore, the methanol diversion device further comprises a float valve, the float valve is positioned between the methanol cache tank and the methanol diversion tank, and as the methanol tail liquid needs one process through rectification and condensation liquefaction, the methanol cache tank is arranged, after more methanol tail liquid is accumulated after rectification, the subsequent diversion and reflux treatment are carried out, so that the methanol purification unit is prevented from being in a continuous working state due to a small amount of methanol tail liquid, and the utilization rate of equipment and energy sources is improved.
As shown in figure 1, the feed inlet of the methanol reflux tank is provided with a methanol feed pump, the discharge outlet of the methanol reflux tank is provided with a methanol extraction pump, and as the top of the reflux tank contains a large amount of water vapor, when methanol flows into the reflux tank at a lower speed, the methanol can be taken away, so that the purity of the methanol is affected, the feed pump can enable the methanol to flow into the reflux tank rapidly, the contact time between the methanol and the water vapor at the top of the reflux tank is reduced, and the methanol is prevented from being polluted by the water vapor. The extraction pump can enable the qualified methanol with purity to flow out to the methanol storage tank rapidly, so that the unqualified methanol entering the reflux tank in the follow-up process is prevented from polluting the qualified methanol.
As shown in FIG. 1, an ammonium chloride tail liquid buffer tank is arranged between the methanol rectifying tower and the separating tank, and because the content of ammonium chloride in the methanol tail liquid is less, the ammonium chloride residual liquid flowing out from the methanol rectifying tower is less, the ammonium chloride residual liquid separated from the methanol rectifying tower is collected by the ammonium chloride tail liquid buffer tank, and then enters an ammonium chloride purifying unit for purification after more ammonium chloride residual liquid is collected, so that the utilization rate of equipment and energy sources is improved.
As shown in figure 1, an auxiliary electric heating tank is further arranged between the ammonium chloride tail liquid buffer tank and the separation tank, the auxiliary electric heating tank is connected with the ammonium chloride buffer tank by means of a heat exchanger, the heat exchanger comprises a first heat exchanger and a second heat exchanger which are mutually connected, the first heat exchanger is connected with a discharge port of the ammonium chloride tail liquid buffer tank, the second heat exchanger is connected with a feed inlet of the separation tank by means of an auxiliary electric heating pipe, the ammonium chloride tail liquid is preheated by the first heat exchanger and the second heat exchanger, if the temperature is higher than 50 ℃, the ammonium chloride tail liquid flows into the separation tank for flash evaporation after passing through the auxiliary electric heating tank, if the temperature is lower than 50 ℃, the ammonium chloride tail liquid firstly flows into the auxiliary electric heating tank for heating to be higher than 50 ℃, then flows into the separation tank for flash evaporation, the ammonium chloride concentrate after flash evaporation enters into a chloroacetic acid crystallization kettle for cooling crystallization, so as to obtain solid ammonium chloride residual liquid, and the ammonium chloride residual liquid is preheated by the heat exchanger and the auxiliary electric heating tank, so that the flash evaporation efficiency in the separation tank is improved.
As shown in fig. 1, a circulating pump is arranged between the separating tank and the second heat exchanger, and the circulating pump can enable the ammonium chloride solution with lower concentration to flow back to the second heat exchanger, and evaporation concentration is performed again, so that the concentration of the ammonium chloride raffinate is improved, and the subsequent cooling crystallization is facilitated.
As shown in figure 1, the separating tank and the second heat exchanger are also provided with a secondary evaporation device, the secondary evaporation device comprises a demister and a compressor, the air inlet end of the demister is connected with the separating tank, the air outlet end of the demister is connected with the second heat exchanger by means of the compressor, the demister enables the secondary steam discharged from the separating tank to contain ammonium chloride solution to flow back into the separating tank, the secondary steam compressor for removing the ammonium chloride solution compresses and forms high-temperature steam, so that the high-temperature steam is used as a heat source of the second heat exchanger to heat ammonium chloride tail liquid, high-temperature condensate is formed by the second heat exchanger, the high-temperature condensate is used as a heat source of the first heat exchanger to preheat the ammonium chloride tail liquid, the process can perfectly utilize the steam in the ammonium chloride purifying unit, energy recycling is formed, the use of the auxiliary electric heating tank is reduced, and energy consumption is reduced.
Claims (7)
1. The utility model provides a glycine production is with methyl alcohol tail liquid processing system, includes methyl alcohol recovery tank, methyl alcohol rectifying column, reboiler, ammonium chloride purification unit and methyl alcohol purification unit, the methyl alcohol recovery tank is connected with the feed inlet of methyl alcohol rectifying column, the feed inlet and the discharge gate of reboiler are connected with the methyl alcohol rectifying column respectively, and the raffinate discharge gate of methyl alcohol rectifying column is connected with ammonium chloride purification unit, the steam discharge gate of methyl alcohol rectifying column is connected with the methyl alcohol purification unit, the ammonium chloride purification unit includes the knockout drum and the chloroacetic acid crystallization kettle who is connected with the knockout drum, the knockout drum is connected with the raffinate discharge gate of methyl alcohol rectifying column, the methyl alcohol purification unit is including condenser, reflux drum and the methyl alcohol holding vessel that connects gradually, the condenser is connected with the gas discharge gate of methyl alcohol rectifying column, the reflux drum's back flow is connected with the methyl alcohol rectifying column, its characterized in that, the methyl alcohol purification unit still includes methyl alcohol diverging device, the condenser is connected with the reflux drum with the methyl alcohol diverging drum with the help of methyl alcohol diverging drum, methyl alcohol diverging drum includes methyl alcohol buffer tank and a plurality of methyl alcohol diverging drums parallelly connected, the feed inlet and reflux drum.
2. The system of claim 1, wherein the methanol splitting device further comprises a ball float valve positioned between the methanol buffer tank and the methanol splitting tank.
3. The system for treating methanol tail liquid for glycine production according to claim 1, wherein a methanol feed pump is arranged at a feed inlet of the methanol reflux tank, and a methanol extraction pump is arranged at a discharge outlet of the methanol reflux tank.
4. The system for treating tail liquid of methanol for glycine production according to claim 1, wherein an ammonium chloride tail liquid buffer tank is arranged between the methanol rectifying tower and the separating tank.
5. The system for treating methanol tail liquid for glycine production according to claim 4, wherein an auxiliary electric heating tank is further arranged between the ammonium chloride tail liquid buffer tank and the separating tank, the auxiliary electric heating tank is connected with the ammonium chloride buffer tank by means of a heat exchanger, the heat exchanger comprises a first heat exchanger and a second heat exchanger which are mutually connected, the first heat exchanger is connected with a discharge port of the ammonium chloride tail liquid buffer tank, and the second heat exchanger is connected with a feed port of the separating tank by means of an auxiliary electric heating pipe.
6. The system for treating methanol tail liquid for glycine production according to claim 5, wherein a circulating pump is provided between the separation tank and the second heat exchanger.
7. The system for treating methanol tail liquid for glycine production according to claim 5, wherein the separation tank and the second heat exchanger are further provided with a secondary evaporation device, the secondary evaporation device comprises a demister and a compressor, an air inlet end of the demister is connected with the separation tank, and an air outlet end of the demister is connected with the second heat exchanger by means of the compressor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223466832.1U CN219072104U (en) | 2022-12-26 | 2022-12-26 | Methanol tail liquid treatment system for glycine production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202223466832.1U CN219072104U (en) | 2022-12-26 | 2022-12-26 | Methanol tail liquid treatment system for glycine production |
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| Publication Number | Publication Date |
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| CN219072104U true CN219072104U (en) | 2023-05-26 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202223466832.1U Active CN219072104U (en) | 2022-12-26 | 2022-12-26 | Methanol tail liquid treatment system for glycine production |
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2022
- 2022-12-26 CN CN202223466832.1U patent/CN219072104U/en active Active
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