CN220194014U - Glycol rectification waste heat recovery and utilization system - Google Patents
Glycol rectification waste heat recovery and utilization system Download PDFInfo
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- CN220194014U CN220194014U CN202321644587.0U CN202321644587U CN220194014U CN 220194014 U CN220194014 U CN 220194014U CN 202321644587 U CN202321644587 U CN 202321644587U CN 220194014 U CN220194014 U CN 220194014U
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 321
- 239000002918 waste heat Substances 0.000 title claims abstract description 154
- 238000011084 recovery Methods 0.000 title claims abstract description 85
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 title claims abstract description 57
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 102
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 69
- 238000007670 refining Methods 0.000 claims abstract description 32
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 29
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 claims description 26
- 238000005245 sintering Methods 0.000 claims description 5
- 238000004821 distillation Methods 0.000 claims 6
- 239000000463 material Substances 0.000 abstract description 29
- 238000004519 manufacturing process Methods 0.000 description 13
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 12
- 238000004064 recycling Methods 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- 230000006872 improvement Effects 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- 239000002699 waste material Substances 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 4
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 150000001298 alcohols Chemical class 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000011112 process operation Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to the field of waste heat recovery and utilization, and particularly discloses a glycol rectification waste heat recovery and utilization system, which comprises a first waste heat boiler communicated with a butanediol removal tower top, a second waste heat boiler communicated with a glycol refining tower top, a third waste heat boiler communicated with a glycol recovery tower top and a recovery steam pipe network, wherein the first waste heat boiler, the second waste heat boiler and the third waste heat boiler are all communicated with a recovery low-pressure steam pipe network, and the recovery steam pipe network is communicated with a steam user; the steam user comprises a methanol removal tower A reboiler, a methanol removal tower B feeding heater, an ethanol light removal tower reboiler and an ethanol refining tower reboiler. By adopting the technical scheme provided by the utility model, the technical problem that the waste heat of the tower top material of the glycol rectifying device is not recycled, so that energy is wasted in the prior art can be solved.
Description
Technical Field
The utility model relates to the field of waste heat recovery and utilization, in particular to a glycol rectification waste heat recovery and utilization system.
Background
The production method of the ethylene glycol mainly comprises two major types of petroleum routes and non-petroleum routes, wherein the petroleum routes are mature in process and wide in application, but are influenced by raw material price and sources, and the production cost is high; but not the synthesis gas in the petroleum route, and the method gradually reflects the advantages of wide and low raw material sources, short process flow, high technical economy and the like, and becomes a research hot spot for the current industrialized preparation of ethylene glycol.
In the process of preparing ethylene glycol from synthesis gas, impurities such as lower carboxylic acid and esters thereof, propylene glycol, butanediol and the like are introduced, and the prepared crude ethylene glycol is required to be rectified to obtain a final ethylene glycol product. Because ethylene glycol is easy to generate dehydration condensation reaction at higher temperature to generate diethylene glycol and triethylene glycol, the temperature is required to be controlled to be lower than 180 ℃ in the rectification operation, and the purity requirement of ethylene glycol products is high (more than 99.9%), a rectification device with multiple towers is often adopted to finish the rectification of crude ethylene glycol through multiple times of decompression.
In the ethylene glycol rectifying device, the butanediol removing tower has the functions of removing butanediol and other trace esters in crude ethylene glycol, the butanediol obtained at the tower top is mixed with ethylene glycol, the ethylene glycol is sent to an ethylene glycol recovery tower to recover the ethylene glycol therein, and the crude ethylene glycol at the tower bottom is pumped to an ethylene glycol refining tower; the ethylene glycol refining tower has the function of further removing light components and heavy components (mainly alcohols such as diethylene glycol, triethylene glycol and the like) in the crude ethylene glycol; the ethylene glycol recovery tower has the function of recovering ethylene glycol, and the mixture containing butanediol obtained from the tower top is sent to a tank area as light dihydric alcohol.
Because the tower top and tower bottom temperatures of the butanediol removing, glycol refining and glycol recycling towers are smaller, namely the tower top materials of the butanediol removing, glycol refining and glycol recycling towers are higher in temperature, water coolers are arranged at the tower tops of the butanediol removing, glycol refining and glycol recycling towers at present in order to reduce the temperature of the partial materials, and the partial high-temperature materials are cooled by adopting circulating water, so that a large amount of circulating water is consumed, the glycol production cost is higher, waste heat loss of the partial materials can be caused, the waste heat is not fully recycled, and the energy waste is caused.
Therefore, there is a need for a glycol rectification waste heat recovery and utilization system to recover and utilize the waste heat of the overhead material in the glycol rectification process, so as to reduce energy waste and reduce the production cost of glycol.
Disclosure of Invention
The utility model aims to provide a glycol rectification waste heat recovery and utilization system, which solves the technical problem that the waste heat of the tower top material of a glycol rectification device is not recovered and utilized, so that energy is wasted in the prior art.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a glycol rectification waste heat recovery and utilization system comprises a first waste heat boiler communicated with a butylene glycol removal tower top, a second waste heat boiler communicated with a glycol refining tower top, a third waste heat boiler communicated with a glycol recovery tower top and a recovery steam pipe network, wherein the first waste heat boiler, the second waste heat boiler and the third waste heat boiler are all communicated with a recovery low-pressure steam pipe network, and the recovery steam pipe network is communicated with a steam user.
The principle and the advantages of the scheme are as follows:
in actual application, materials (butanediol mixed with ethylene glycol) at the top of the butanediol removing tower pass through a first waste heat boiler, and the waste heat of the materials is recycled by the first waste heat boiler to produce steam; materials (mainly alcohols such as diethylene glycol, triethylene glycol and the like) at the top of the ethylene glycol refining tower pass through a second waste heat boiler, and the waste heat of the materials is recycled by the second waste heat boiler to produce steam; the materials (mixture containing butanediol) at the top of the glycol recovery tower pass through a third waste heat boiler, and the third waste heat boiler recovers and utilizes the waste heat of the materials to produce steam; and the steam produced by the first waste heat boiler, the second waste heat boiler and the third waste heat boiler is fed into a recovery steam pipe network and is conveyed to a steam user by the recovery steam pipe network for use by the steam user.
According to the scheme, the waste heat of materials at the top of each tower is recovered through the first waste heat boiler, the second waste heat boiler and the third waste heat boiler which are communicated with the butylene glycol removal tower, the ethylene glycol refining tower and the ethylene glycol recovery tower, and steam is produced by utilizing the waste heat for a steam user, namely, on the basis of not changing the structure of an original ethylene glycol rectifying device, the waste heat boiler is additionally arranged at each tower top, so that the recycling of the waste heat of the materials at the top of each tower can be realized, and the waste of energy sources is effectively avoided.
Before using this scheme to recycle the residual heat of the material at the top of the glycol rectifying device, the inventors have tried the following scheme: the method comprises the steps of respectively connecting a first waste heat boiler, a second waste heat boiler and a third waste heat boiler at the tops of a butanediol removal tower, an ethylene glycol refining tower and an ethylene glycol recovery tower, and correspondingly connecting the first waste heat boiler, the second waste heat boiler and the third waste heat boiler with a steam user one by one, so that steam produced by recycling waste heat of materials at the tops of the first waste heat boiler, the second waste heat boiler and the third waste heat boiler is supplied to the steam user one by one. But the inventors found in testing the protocol that: the waste heat quantity which can be recycled by the waste heat boilers positioned at different tower tops is different, so that the steam quantity generated by each waste heat boiler is different, and the steam quantity is difficult to match with the steam demand of a steam user when the waste heat boilers are supplied to the steam user one by one; and along with the promotion of glycol rectification process, the waste heat of the tower top material can change, so that the steam quantity which can be produced by the corresponding waste heat boiler fluctuates, and the stability of the steam quantity supplied by a steam user is difficult to ensure.
By adopting the scheme, the recovery steam pipe network is additionally arranged, the steam produced by recycling the waste heat of the corresponding tower top materials of the first waste heat boiler, the second waste heat boiler and the third waste heat boiler is firstly introduced into the recovery steam pipe network, and after the steam produced by each waste heat boiler is collected in the recovery steam pipe network, the steam is respectively supplied to each steam user, so that the stability of the steam quantity supplied to each steam user can be ensured; and the steam produced by each waste heat boiler is collected in the recovery steam pipe network and then is supplied in the same way, so that the quality (pressure and temperature) of the steam used by a steam user can be improved to be more stable, and stable process operation at the steam user can be ensured.
Preferably, as an improvement, the steam user comprises a methanol removal tower A reboiler, and the methanol removal tower A reboiler is communicated with the methanol removal tower A of the ethylene glycol rectifying device.
By adopting the scheme, steam generated by recycling waste heat of tower top materials of a butanediol removal tower, a glycol refining tower and a glycol recovery tower in the glycol rectifying device enters a recovery steam pipe network, and is fed to a methanol removal tower A in the glycol rectifying device through the recovery steam pipe network for being used by a reboiler of the methanol removal tower A, and partial external steam can be replaced by steam generated by recycling the waste heat of the glycol rectification, so that the using amount of the external steam is reduced, the overall energy consumption of the glycol rectification is reduced, and the production cost of the glycol is saved.
Preferably, as an improvement, the steam user further comprises a methanol removal tower B feeding heater, and the methanol removal tower B feeding heater is communicated with a methanol removal tower B of the ethylene glycol rectifying device.
By adopting the scheme, steam generated by the recovery of waste heat of materials at the top of a butylene glycol removal tower, a ethylene glycol refining tower and an ethylene glycol recovery tower in the ethylene glycol rectifying device enters a recovery steam pipe network, and is fed to a methanol removal tower B in the ethylene glycol rectifying device through the recovery steam pipe network for a methanol removal tower B feeding heater to use, and steam generated by the recovery of waste heat of ethylene glycol feeding can replace part of external steam, so that the using amount of external steam is further reduced, the overall energy consumption of ethylene glycol rectification is further reduced, and the production cost of ethylene glycol is saved.
Preferably, as an improvement, the steam user further comprises an ethanol light-removal tower reboiler, and the ethanol light-removal tower reboiler is communicated with the ethanol light-removal tower of the ethylene glycol rectifying device.
By adopting the scheme, the steam generated by the recovery of the waste heat of the materials at the top of the butanediol removing tower, the ethylene glycol refining tower and the ethylene glycol recovery tower in the ethylene glycol rectifying device enters the recovery steam pipe network, and is fed to the ethanol light removal tower in the ethylene glycol rectifying device through the recovery steam pipe network for the reboiler of the ethanol light removal tower to use, and the steam generated by the recovery of the waste heat of the ethylene glycol feeding can replace part of external steam, so that the using amount of the external steam is further reduced, the overall energy consumption of the ethylene glycol rectifying is further reduced, and the production cost of the ethylene glycol is saved.
Preferably, as an improvement, the steam user further comprises an ethanol refining tower reboiler, and the ethanol refining tower reboiler is communicated with the ethanol refining tower of the ethylene glycol rectifying device.
By adopting the scheme, the steam generated by the recovery of the waste heat of the materials at the top of the butanediol removal tower, the ethylene glycol refining tower and the ethylene glycol recovery tower in the ethylene glycol rectifying device enters the recovery steam pipe network, and is fed to the ethanol refining tower in the ethylene glycol rectifying device through the recovery steam pipe network for the reboiler of the ethanol refining tower to use, and the steam generated by the recovery of the waste heat of the ethylene glycol feeding can replace part of external steam, so that the using amount of the external steam is further reduced, the overall energy consumption of the ethylene glycol rectification is further reduced, and the production cost of the ethylene glycol is saved.
Preferably, as an improvement, the first waste heat boiler, the second waste heat boiler and the third waste heat boiler all adopt sintering type high-flux heat exchange tubes.
By adopting the scheme, the first waste heat boiler, the second waste heat boiler and the third waste heat boiler all adopt the sintering type high-flux heat exchange tubes, compared with the common heat exchange tubes, the sintering type high-flux heat exchange tubes can improve the heat exchange coefficients of the first waste heat boiler, the second waste heat boiler and the third waste heat boiler, so that the heat exchange coefficients of the first waste heat boiler, the second waste heat boiler and the third waste heat boiler reach more than twice that of the common heat exchange tubes, the utilization rate of the material waste heat at the top of the ethylene glycol rectifying device is improved, the waste of energy sources is further reduced, more steam is produced for the recycling of the ethylene glycol rectifying device, and the production cost is further saved.
Preferably, as an improvement, the methanol removal tower A reboiler, the methanol removal tower B feed heater, the ethanol light removal tower reboiler and the ethanol refining tower reboiler are all communicated with a lithium bromide refrigerating unit, the lithium bromide refrigerating unit is communicated with a deaerator, the deaerator is communicated with a boiler water pipe network, and the boiler water pipe network is communicated with a first waste heat boiler, a second waste heat boiler and a third waste heat boiler.
By adopting the scheme, the lithium bromide refrigerating unit is communicated with the steam user methanol removal tower A reboiler, the methanol removal tower B feed heater, the ethanol light removal tower reboiler and the ethanol refining tower reboiler, the steam condensate after being used by the steam user is introduced into the lithium bromide refrigerating unit, the low temperature water is further cooled after being prepared to form condensed water, then oxygen and other gases in the condensed water are removed by the deaerator, the deoxidized water is obtained and is introduced into the boiler water pipe network, and the boiler water pipe network supplies the condensed water to the first waste heat boiler, the second waste heat boiler and the third waste heat boiler for use, so that the cyclic use of water resources is realized, the resource consumption is reduced, and the production cost of ethylene glycol is further saved. The lithium bromide refrigerating unit is used for cooling the steam condensate after the steam user uses, so that the water resource can be reused, the lithium bromide refrigerating unit can be used for preparing low-temperature water by utilizing the waste heat in the steam, and the waste of energy sources is further reduced.
Preferably, as an improvement, the recovery steam pipe network is communicated with an external steam pipe network, and the external steam pipe network is communicated with an external steam source.
By adopting the scheme, the external steam pipe network is communicated on the recovery steam pipe network, when the glycol rectifying device is in an on-off or fault state and the steam yield is unstable, the external steam pipe network is utilized to convey the steam of the external steam source into the recovery steam pipe network, the unstable steam quantity in the recovery steam pipe network is supplemented, the stability of the recovery steam pipe network for the steam user to supply the steam quantity can be ensured, and thus the stable process operation of the steam user is ensured.
Drawings
Fig. 1 is a schematic structural diagram of embodiment 1 of the present utility model.
Detailed Description
The following is a further detailed description of the embodiments:
reference numerals in the drawings of the specification include: 1 butanediol removing tower, 2 ethylene glycol refining tower, 3 ethylene glycol recovery tower, 4 first waste heat boiler, 5 second waste heat boiler, 6 third waste heat boiler, 7 recovery steam pipe network, 8 methanol removing tower A reboiler, 9 methanol removing tower B feeding heater, 10 ethanol light tower reboiler, 11 ethanol refining tower reboiler.
Example 1
A glycol rectification waste heat recovery and utilization system is shown in figure 1, and comprises a first waste heat boiler 4 communicated with the top of a butylene glycol removal tower 1 through a pipeline, a second waste heat boiler 5 communicated with the top of a glycol refining tower 2 through a pipeline, a third waste heat boiler 6 communicated with the top of a glycol recovery tower 3 through a pipeline and a recovery steam pipe network 7, wherein the first waste heat boiler 4, the second waste heat boiler 5 and the third waste heat boiler 6 are all communicated with a recovery low-pressure steam pipe network, and the recovery steam pipe network 7 is communicated with a steam user.
In this embodiment, the steam user includes a methanol removal tower a reboiler 8, a methanol removal tower B feed heater 9, an ethanol light removal tower reboiler 10, and an ethanol purification tower reboiler 11, wherein the methanol removal tower a reboiler 8 is communicated with a methanol removal tower a of the ethylene glycol rectification device, the methanol removal tower B feed heater 9 is communicated with a methanol removal tower B of the ethylene glycol rectification device, the ethanol light removal tower reboiler 10 is communicated with an ethanol light removal tower of the ethylene glycol rectification device, and the ethanol purification tower reboiler 11 is communicated with an ethanol purification tower of the ethylene glycol rectification device.
In this embodiment, the first waste heat boiler 4, the second waste heat boiler 5 and the third waste heat boiler 6 all adopt sintering type high flux heat exchange tubes, and compared with the common heat exchange tubes, the heat exchange efficiency can reach more than twice. The recovery steam pipe network 7 can be communicated with other steam users in the glycol rectification process and is used for supplying steam to the recovery steam pipe network, so that the glycol rectification energy consumption is further reduced, and the production cost is saved; the recovery steam pipe network 7 can be communicated with an external steam user even and is used for treating the steam which is not used up by the glycol rectifying device, so that energy waste is avoided.
The specific implementation process is as follows:
waste heat recovery and utilization: the material (butanediol mixed with ethylene glycol) at the top of the butanediol removal tower 1 passes through a first waste heat boiler 4, and the waste heat of the material is recycled by the first waste heat boiler 4 to produce steam; materials (mainly alcohols such as diethylene glycol, triethylene glycol and the like) at the top of the ethylene glycol refining tower 2 pass through a second waste heat boiler 5, and the waste heat of the materials is recycled by the second waste heat boiler 5 to produce steam; the materials (mixture containing butanediol) at the top of the glycol recovery tower 3 pass through a third waste heat boiler 6, and the third waste heat boiler 6 is used for producing steam by recycling the waste heat; the steam produced by the first waste heat boiler 4, the second waste heat boiler 5 and the third waste heat boiler 6 is all led into a recovery steam pipe network 7.
Steam feed use: the recovery steam pipe network 7 respectively supplies the steam collected from the first waste heat boiler 4, the second waste heat boiler 5 and the third waste heat boiler 6 to a methanol removal tower A reboiler 8, a methanol removal tower B feeding heater 9, an ethanol light removal tower reboiler 10 and an ethanol refining tower reboiler 11 in the ethylene glycol rectifying device for the steam users of the ethylene glycol rectifying device, and the steam produced by recycling the waste heat of the ethylene glycol rectification replaces part of external steam, so that the use amount of the external steam is reduced, the whole energy consumption of the ethylene glycol rectification can be reduced, and the ethylene glycol production cost is saved.
Example 2
The difference between the glycol rectification waste heat recovery and utilization system and the embodiment 1 is that: the recovery steam pipe network 7 is communicated with an external steam pipe network, and the external steam pipe network is communicated with an external steam source. Specifically, the external steam source may adopt a steam generator, a steam boiler, etc., which is the prior art, and this embodiment will not be described in detail.
According to the scheme, the external steam pipe network is communicated with the recovery steam pipe network 7, when the glycol rectifying device is in an on-off or fault state and the steam yield is unstable, the external steam pipe network is utilized to convey steam of an external steam source into the recovery steam pipe network 7, the unstable steam quantity in the recovery steam pipe network 7 is supplemented, the stability of the recovery steam pipe network 7 for supplying the steam quantity to a steam user can be guaranteed, and therefore stable process operation of the steam user is guaranteed.
Example 3
The difference between the glycol rectification waste heat recovery and utilization system and the embodiment 1 is that: the reboiler of the methanol removal tower A, the feed heater of the methanol removal tower B, the reboiler 10 of the ethanol removal tower and the reboiler 11 of the ethanol refining tower are all communicated with a lithium bromide refrigerating unit through pipelines, the lithium bromide refrigerating unit is communicated with a deaerator through pipelines, the deaerator is communicated with a boiler water pipe network, and the boiler water pipe network is communicated with the first waste heat boiler 4, the second waste heat boiler 5 and the third waste heat boiler 6.
In the scheme, the steam condensate after being used by a steam user is introduced into a lithium bromide refrigerating unit, the low-temperature water is prepared and then is further cooled to form condensate water, then oxygen and other gases in the condensate water are removed through a deaerator, the obtained deoxidized water is introduced into a boiler water pipe network, and the boiler water pipe network supplies the condensate water to a first waste heat boiler, a second waste heat boiler and a third waste heat boiler for use, so that the cyclic use of water resources is realized, the resource consumption is reduced, and the production cost of ethylene glycol is further saved. The lithium bromide refrigerating unit is used for cooling the steam condensate after the steam user uses, so that the water resource can be reused, the lithium bromide refrigerating unit can be used for preparing low-temperature water by utilizing the waste heat in the steam, and the waste of energy sources is further reduced.
The foregoing is merely exemplary of the present utility model, and specific technical solutions and/or features that are well known in the art have not been described in detail herein. It should be noted that, for those skilled in the art, several variations and modifications can be made without departing from the technical solution of the present utility model, and these should also be regarded as the protection scope of the present utility model, which does not affect the effect of the implementation of the present utility model and the practical applicability of the patent. The protection scope of the present application shall be subject to the content of the claims, and the description of the specific embodiments and the like in the specification can be used for explaining the content of the claims.
Claims (8)
1. A glycol rectification waste heat recovery and utilization system is characterized in that: the system comprises a first waste heat boiler communicated with the top of a butanediol removing tower, a second waste heat boiler communicated with the top of a glycol refining tower, a third waste heat boiler communicated with the top of a glycol recovery tower and a recovery steam pipe network, wherein the first waste heat boiler, the second waste heat boiler and the third waste heat boiler are all communicated with a recovery low-pressure steam pipe network, and the recovery steam pipe network is communicated with a steam user.
2. The glycol distillation waste heat recovery and utilization system according to claim 1, wherein: the steam user comprises a methanol removal tower A reboiler which is communicated with a methanol removal tower A of the glycol rectifying device.
3. The glycol distillation waste heat recovery and utilization system according to claim 2, wherein: the steam user also comprises a methanol removal tower B feeding heater which is communicated with the methanol removal tower B of the glycol rectifying device.
4. A glycol rectification waste heat recovery and utilization system according to claim 3, wherein: the steam user also comprises an ethanol light component removing tower reboiler which is communicated with the ethanol light component removing tower of the glycol rectifying device.
5. The glycol distillation waste heat recovery and utilization system according to claim 4, wherein: the steam user also comprises an ethanol refining tower reboiler which is communicated with the ethanol refining tower of the glycol rectifying device.
6. The glycol distillation waste heat recovery and utilization system according to claim 5, wherein: the first waste heat boiler, the second waste heat boiler and the third waste heat boiler all adopt sintering type high-flux heat exchange tubes.
7. The glycol distillation waste heat recovery and utilization system according to claim 6, wherein: the reboiler of the methanol removal tower A, the feed heater of the methanol removal tower B, the reboiler of the ethanol removal tower and the reboiler of the ethanol refining tower are all communicated with a lithium bromide refrigerating unit, the lithium bromide refrigerating unit is communicated with a deaerator, the deaerator is communicated with a boiler water pipe network, and the boiler water pipe network is communicated with a first waste heat boiler, a second waste heat boiler and a third waste heat boiler.
8. The glycol distillation waste heat recovery and utilization system according to any one of claims 1-7, wherein: the recovery steam pipe network is communicated with an external steam pipe network, and the external steam pipe network is communicated with an external steam source.
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| CN202321644587.0U CN220194014U (en) | 2023-06-26 | 2023-06-26 | Glycol rectification waste heat recovery and utilization system |
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| CN202321644587.0U CN220194014U (en) | 2023-06-26 | 2023-06-26 | Glycol rectification waste heat recovery and utilization system |
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| GR01 | Patent grant |