CN106839651A - The system and technique of nitrogen are reclaimed in a kind of tail gas from vacuum drying oven - Google Patents
The system and technique of nitrogen are reclaimed in a kind of tail gas from vacuum drying oven Download PDFInfo
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- CN106839651A CN106839651A CN201710187942.9A CN201710187942A CN106839651A CN 106839651 A CN106839651 A CN 106839651A CN 201710187942 A CN201710187942 A CN 201710187942A CN 106839651 A CN106839651 A CN 106839651A
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- Prior art keywords
- gas
- vacuum drying
- tail gas
- drying oven
- nitrogen
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Links
- 239000007789 gas Substances 0.000 title claims abstract description 177
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 238000001291 vacuum drying Methods 0.000 title claims abstract description 56
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 51
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 115
- 238000001816 cooling Methods 0.000 claims abstract description 62
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 claims abstract description 30
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 claims abstract description 26
- 238000007906 compression Methods 0.000 claims abstract description 24
- 230000006835 compression Effects 0.000 claims abstract description 23
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 claims abstract description 13
- 239000012530 fluid Substances 0.000 claims description 58
- 238000000926 separation method Methods 0.000 claims description 33
- 230000002977 hyperthermial effect Effects 0.000 claims description 11
- 238000004064 recycling Methods 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 4
- 238000005057 refrigeration Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 abstract description 7
- 239000011261 inert gas Substances 0.000 abstract description 4
- 230000001681 protective effect Effects 0.000 description 8
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- GEDCQGWBCURDLS-UHFFFAOYSA-N [N].CCOC(C)=O Chemical compound [N].CCOC(C)=O GEDCQGWBCURDLS-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 229910052786 argon Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000008542 thermal sensitivity Effects 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/062—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0219—Refinery gas, cracking gas, coke oven gas, gaseous mixtures containing aliphatic unsaturated CnHm or gaseous mixtures of undefined nature
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/066—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/12—Refinery or petrochemical off-gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/44—Separating high boiling, i.e. less volatile components from nitrogen, e.g. CO, Ar, O2, hydrocarbons
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Drying Of Gases (AREA)
Abstract
The invention discloses system and technique that nitrogen is reclaimed in a kind of tail gas from vacuum drying oven, belong to vacuum drying oven tail gas recycle process field, can effectively reclaim nitrogen from the vacuum drying oven tail gas containing the composition such as tetrahydrofuran and/or ethyl acetate；The system is including surge tank, compressor, the first cooler, the first gas-liquid separator, First Heat Exchanger, the second cooler, the second gas-liquid separator, the second heat exchanger, the 3rd gas-liquid separator and choke valve etc..Simple system of the invention, by carrying out the compression of early stage and follow-up multiple cooling, separating treatment to vacuum drying oven tail gas, the compositions such as tetrahydrofuran and/or ethyl acetate contained in vacuum drying oven tail gas can be efficiently separated, and then the inert gases such as the nitrogen in vacuum drying oven tail gas can effectively be recycled, improve the resource utilization of the inert gases such as nitrogen.In addition, the present invention also realizes maximally utilizing for efficiency, and then reduce operating cost.
Description
Technical field
Returned from vacuum drying oven tail gas the present invention relates to vacuum drying oven tail gas recycle processing technology field, more particularly to one kind
Receive the system and technique of nitrogen.
Background technology
Vacuum drying oven is that a kind of aiming at dries thermal sensitivity or containing solvent and need the drying equipment of recycling design material, and
And can be to being filled with the protective gas such as nitrogen inside it to cause oxygen to article in preventing drying process during dry goods
Change is acted on.Current vacuum drying oven has been widely used for the work drying of the industries such as medicine, food, light industry, chemical industry, electronics and is used, its tool
Have the advantages that dry goods speed is fast, pollute inherent qualities small, not to dried object product to damage.
But, when being dried to some articles for containing specific solvent using vacuum drying oven, such as contain tetrahydrofuran
Or the article of ethyl acetate equal solvent is when being dried, the tail discharged from vacuum drying oven after treatment is dried to article
In gas in addition to containing protective gas such as nitrogen, can also contain the components such as a certain amount of tetrahydrofuran or ethyl acetate, and
It is also possible to contain a certain amount of gaseous state water component.And due to containing the component such as tetrahydrofuran or ethyl acetate, causing from vacuum
The protective gas such as contained nitrogen component can not directly be recycled in the tail gas that baking oven is discharged, and thus result in nitrogen etc.
The waste of protective gas.
The content of the invention
Present invention solves the technical problem that be to provide it is a kind of can be from containing the composition such as tetrahydrofuran and/or ethyl acetate
The system and technique of nitrogen are reclaimed in vacuum drying oven tail gas.
The technical solution adopted for the present invention to solve the technical problems is：Nitrogen is reclaimed in a kind of tail gas from vacuum drying oven
System, including
Surge tank, the surge tank is connected with the tail gas outlet of vacuum drying oven；
Compressor, the entrance of the compressor is connected with surge tank；
First cooler, the entrance of first cooler and the outlet of compressor；
First gas-liquid separator, the entrance of first gas-liquid separator and the outlet of the first cooler；
First Heat Exchanger, is provided with the first thermal fluid inlet, the first hot fluid outlet ports, the first cold flow on First Heat Exchanger
Body entrance and the first cold fluid outlet；First thermal fluid inlet is connected with the gas vent on the first gas-liquid separator；
Second cooler, the entrance of second cooler is connected with the first hot fluid outlet ports；
Second gas-liquid separator, the entrance of second gas-liquid separator and the outlet of the second cooler；
Second heat exchanger, is provided with the second thermal fluid inlet, the second hot fluid outlet ports, the second cold flow on the second heat exchanger
Body entrance and the second cold fluid outlet；Second thermal fluid inlet is connected with the gas vent on the second gas-liquid separator；
3rd gas-liquid separator, the entrance of the 3rd gas-liquid separator is connected with the second hot fluid outlet ports；And the 3rd
Gas vent on gas-liquid separator is connected with the second cold fluid inlet；
Choke valve, one end of the choke valve connects with the second cold fluid outlet, the other end of choke valve and described first
Cold fluid inlet is connected；
First cold fluid outlet is nitrogen recycling port.
It is further：In the bottom of the first gas-liquid separator, the second gas-liquid separator and the 3rd gas-liquid separator three
Waste liquid outlet is respectively arranged with, and the waste liquid outlet is connected with sewer pipe respectively.
It is further：The First Heat Exchanger and the second heat exchanger are plate-fin heat exchanger.
It is further：First cooler is air cooler or water cooling heat exchanger, and second cooler is refrigeration machine.
In addition, the present invention reclaims the technique of nitrogen in also providing a kind of tail gas from vacuum drying oven, using the invention described above institute
The system that nitrogen is reclaimed from vacuum drying oven tail gas stated, for from the vacuum drying oven containing tetrahydrofuran and/or ethyl acetate
Nitrogen is reclaimed in tail gas, is comprised the following steps：
A. the tail gas discharged from the tail gas outlet of vacuum drying oven obtains buffered in surge tank first；
B. enter compressor by the tail gas after buffered and processed by compression；
C. the tail gas after being processed through overcompression enters the first cooler and is processed by first time cooling；
D. enter the first gas-liquid separator by the tail gas after first time cooling treatment and processed by first time gas-liquid separation；
E. First Heat Exchanger is entered and by second cooling treatment by the gas part after first time gas-liquid separation treatment；
F. enter the second cooler by the gas after second cooling treatment and processed by third time cooling；
G. the second gas-liquid separator is entered and by second gas-liquid separation treatment by the gas after third time cooling treatment；
H. the second heat exchanger is entered and by the 4th cooling treatment by the gas part after second gas-liquid separation treatment；
I. enter the 3rd gas-liquid separator by the gas after the 4th cooling treatment and processed by third time gas-liquid separation；
J. by third time gas-liquid separation treatment after gas part into choke valve and be depressurized to 110kPa.A~
250kPa.A, while by the 5th cooling treatment；
K. the second heat exchanger is entered and by first time hyperthermic treatment by the gas of choke valve；
L. First Heat Exchanger is entered and by second hyperthermic treatment by the gas after first time hyperthermic treatment, by second
Gas after secondary hyperthermic treatment is discharged from nitrogen recycling port.
It is further：0.5MPa.A is not less than by the air pressure of the tail gas after compressor compresses treatment.
It is further：The temperature of the tail gas after first time cooling is processed is 30 DEG C~50 DEG C.
It is further：The temperature of the gas after second cooling is processed is -30 DEG C~-5 DEG C.
It is further：The temperature of the gas after third time cooling is processed is -50 DEG C~-35 DEG C.
It is further：The temperature of the gas after the 4th cooling is processed is -80 DEG C~-65 DEG C.
The beneficial effects of the invention are as follows：Simple system of the present invention, early stage is carried out by vacuum drying oven tail gas
Compression and follow-up multiple cooling, separating treatment, can be by tetrahydrofuran contained in vacuum drying oven tail gas and/or acetic acid second
The compositions such as ester are efficiently separated, and then can effectively be reclaimed profit to protective gas such as the nitrogen in vacuum drying oven tail gas
With improve the resource utilization of the protective gas such as nitrogen.In addition, only needing to be processed by the compression of first compression machine in the present invention
The active cooling treatment of cooler twice needs extra consumption energy consumption, and without additional energy in remaining processing procedure, and
And by cryogenic cold energy entrained in the nitrogen reclaimed after reusing final separation, also can reach the maximization profit of efficiency
With, therefore the energy resource consumption of whole system can be also to greatest extent reduced, and then reduce operating cost.
Brief description of the drawings
Fig. 1 is the annexation schematic diagram of the system of recovery nitrogen in a kind of tail gas from vacuum drying oven of the present invention；
Marked in figure：Vacuum drying oven 1, surge tank 2, compressor 3, the first cooler 4, the first gas-liquid separator 5, first
Heat exchanger 6, the first thermal fluid inlet 61, the first hot fluid outlet ports 62, the first cold fluid inlet 63, the first cold fluid outlet 64,
Second cooler 7, the second gas-liquid separator 8, the second heat exchanger 9, the second thermal fluid inlet 91, the second hot fluid outlet ports 92,
Two cold fluid inlets 93, the second cold fluid outlet 94, the 3rd gas-liquid separator 10, choke valve 11, sewer pipe 12.
Specific embodiment
The present invention is further described with reference to the accompanying drawings and detailed description.Heretofore described vacuum drying oven tail
What gas referred to dries the tail gas discharged after respective articles from vacuum drying oven 1；And the present invention be directed in tail gas except containing
Have outside the protective gas such as nitrogen, the treatment of the mixed tail gas also containing the composition such as tetrahydrofuran and/or ethyl acetate, to reclaim tail
Nitrogen in gas.
As shown in fig. 1, the system that nitrogen is reclaimed in a kind of tail gas from vacuum drying oven of the present invention, including
Surge tank 2, the surge tank 2 is connected with the tail gas outlet of vacuum drying oven 1；
Compressor 3, the entrance of the compressor 3 is connected with surge tank 2；
First cooler 4, the entrance of first cooler 4 and the outlet of compressor 3；
The outlet of the first gas-liquid separator 5, the entrance of first gas-liquid separator 5 and the first cooler 4；
First Heat Exchanger 6, is provided with the first thermal fluid inlet 61, the first hot fluid outlet ports 62, on First Heat Exchanger 6
One cold fluid inlet 63 and the first cold fluid outlet 64；Gas on the gas-liquid separator 5 of first thermal fluid inlet 61 and first
Body outlet；
Second cooler 7, the entrance of second cooler 7 is connected with the first hot fluid outlet ports 62；
The outlet of the second gas-liquid separator 8, the entrance of second gas-liquid separator 8 and the second cooler 7；
Second heat exchanger 9, is provided with the second thermal fluid inlet 91, the second hot fluid outlet ports 92, on the second heat exchanger 9
Two cold fluid inlets 93 and the second cold fluid outlet 94；Gas on the gas-liquid separator 8 of second thermal fluid inlet 91 and second
Body outlet；
3rd gas-liquid separator 10, the entrance of the 3rd gas-liquid separator 10 is connected with the second hot fluid outlet ports 92；And
And the 3rd gas vent on gas-liquid separator 10 is connected with the second cold fluid inlet 93；
Choke valve 11, one end of the choke valve 11 connects with the second cold fluid outlet 94, the other end of choke valve 11 with
First cold fluid inlet 63 is connected；
First cold fluid outlet 64 is nitrogen recycling port.
Specific workflow of the invention is：The tail gas discharged from vacuum drying oven 1 is discharged into surge tank 2 first,
And the buffered of certain effect is realized by surge tank 2, and interim storage purpose can be carried out to tail gas；Then tail gas enters
Processed with by compression in compressor 3, and the temperature of tail gas will be raised after compression treatment；Then after compression is processed again
Tail gas be passed into the first cooler 4 in carry out cooling treatment so that the tail gas after compression is lowered the temperature, under normal circumstances will be through
The tail gas crossed after the first cooler 4 is cooled to normal temperature nearby；Then the tail gas after above-mentioned cooling is processed is passed into first
Gas-liquid separator 5 carries out first time gas-liquid separation；Afterwards further by the cooler 7 of First Heat Exchanger 6 and second carry out to from
The gas part that first gas-liquid separator 5 is isolated carries out continuous cooling treatment, and by by the gas after the treatment of cooling twice
Being passed into again in the second gas-liquid separator 8 carries out second gas-liquid separation；Carried out to from second by the second heat exchanger 9 again afterwards
The gas part that gas-liquid separator 8 is isolated carries out cooling treatment again, and gas after cooling is processed again is passed into the 3rd
Third time gas-liquid separation is carried out in gas-liquid separator 10；Afterwards again by choke valve 11 by from the 3rd gas-liquid separator 10 discharge
Gas part carries out pressure release treatment, after the pressure release of above-mentioned choke valve 11 is processed, on the one hand can make the portion gas recover to
Close to the pressure of normal pressure, the temperature of the portion gas on the other hand can be further reduced.And in above process, the first heat exchange
Low-temperature receiver in the heat exchanger 9 of device 6 and second is provided by the gas part after lowering the temperature through the pressure release of choke valve 11, is so capable of achieving to this
The effective recycling of the cold energy in portion gas, and then the operation energy consumption of whole equipment is reduced, reach the purpose for economizing on resources.
In addition, it is necessary to illustrate, " tail gas " or " gas " for describing in the present invention is for only for ease of description, and
It is not used to limit the physical state of tie substance；It is theoretical for example in tail gas after being cooled to normal temperature after the first cooler 4
On in the tail gas in addition to containing gaseous nitrogen, can also contain a certain amount of aqueous water, liquid tetrahydrofuran and/or liquid
State ethyl acetate etc., but substantially it is in vaporific due to corresponding liquid composition, therefore it is mixed to be still referred to as this with " tail gas " in the present invention
Compound.
In addition, the first gas-liquid separator 5, the second gas-liquid separator 8 and the 3rd gas-liquid separator 10 are for corresponding
The equipment that liquid composition in gas is separate, the liquid portion for isolating can be initially stored in correspondence gas-liquid separator
Bottom, then discharged being collected by corresponding waste liquid outlet again；Specifically, can refer to shown in accompanying drawing 1, one can be entered
Step is respectively arranged with waste liquid in the bottom of the first gas-liquid separator 5, the second gas-liquid separator 8 and the three of the 3rd gas-liquid separator 10
Outlet, and sewer pipe 12 can be further provided with, while the waste liquid outlet is connected with sewer pipe 12 respectively；Can so lead to
Cross sewer pipe 12 and directly collect the liquid portion that above three gas-liquid separator is discharged.
In addition, the heat exchanger 9 of First Heat Exchanger 6 and second in the invention described above, lets out the purpose is to utilize through choke valve 11
The cold energy of the gas part after pressure drop temperature, and then effective recycling of the realization to the cold energy of portion gas carrying, reach drop
Low system overall operation energy consumption, the purpose for economizing on resources.Without loss of generality, the First Heat Exchanger 6 and second in the present invention exchanges heat
Device 9 can such as use plate-fin heat exchanger using conventional heat exchanger.
In addition, the first cooler 4 in the invention described above, the purpose is to be used for by after the compression of compressor 3 treatment
Tail gas carries out cooling treatment.Under normal circumstances, the temperature of the tail gas discharged from vacuum drying oven is general at 30 DEG C to 40 DEG C or so,
And by after the compression treatment of compressor 3, its temperature can also be raised further in theory, and due to compression ratio and compression process
In the influence therefore such as thermal loss, the gas temperature after Normal squeezing can reach more than 100 DEG C, it is therefore desirable to from corresponding
The first cooler 4 so that the gas temperature after compression effectively can be down to required temperature by it.In addition, according to compression ratio
Difference, compressor 3 may be configured as the processing mode of one stage of compression or two-stage compression or multi-stage compression, by vacuum drying oven tail
Air pressure is reduced to required pressure.
Specifically, needing for tail gas to be cooled to normal temperature after generally going through the cooling treatment of the first cooler 4 in the present invention attached
Closely, 30 DEG C~50 DEG C are such as cooled to；As long as meeting the cooler 4 of above-mentioned requirements in theory, air cooler or water can be such as used
Cold heat exchanger is used as the first cooler 4.In addition, the second cooler 7 in the present invention, it is for by First Heat Exchanger 6
Gas afterwards is further lowered the temperature, and generally goes through the temperature needs of the gas after the cooling treatment of the second cooler 7
Reach in the range of -50 DEG C~-35 DEG C, as long as therefore meeting the cooler of above-mentioned requirements in theory；Refrigeration machine can such as be used
As the second cooler 7.
In addition, the present invention reclaims the technique of nitrogen in also providing a kind of tail gas from vacuum drying oven, using the invention described above institute
The system that nitrogen is reclaimed from vacuum drying oven tail gas stated, for from the vacuum drying oven containing tetrahydrofuran and/or ethyl acetate
Nitrogen is reclaimed in tail gas, is comprised the following steps：
A. the tail gas discharged from the tail gas outlet of vacuum drying oven 1 obtains buffered in surge tank 2 first；
B. enter compressor 3 by the tail gas after buffered and processed by compression；
C. the tail gas after being processed through overcompression enters the first cooler 4 and is processed by first time cooling；
D. the first gas-liquid separator 5 is entered and by first time gas-liquid separation by the tail gas after first time cooling treatment
Reason；
E. First Heat Exchanger 6 is entered and by second cooling by the gas part after first time gas-liquid separation treatment
Reason；
F. enter the second cooler 7 by the gas after second cooling treatment and processed by third time cooling；
G. the second gas-liquid separator 8 is entered and by second gas-liquid separation by the gas after third time cooling treatment
Reason；
H. the second heat exchanger 9 is entered and by the 4th cooling by the gas part after second gas-liquid separation treatment
Reason；
I. the 3rd gas-liquid separator 10 is entered and by third time gas-liquid separation by the gas after the 4th cooling treatment
Reason；
J. by third time gas-liquid separation treatment after gas part enter choke valve 11, and be depressurized to 110kPa.A~
250kPa.A, while by the 5th cooling treatment；
K. the second heat exchanger 9 is entered and by first time hyperthermic treatment by the gas of choke valve 11；
L. First Heat Exchanger 6 is entered and by second hyperthermic treatment by the gas after first time hyperthermic treatment, by the
Gas after secondary temperature elevation treatment is discharged from nitrogen recycling port.
More specifically, due in above-mentioned technique, it is necessary to reuse the gas part after eventually passing choke valve 11
For having by the cold fluid and the temperature of hot fluid in the heat exchanger 9 of First Heat Exchanger 6 and second in cold energy, therefore the present invention
Certain area requirement, cannot otherwise ensure effective operation of whole system.And consider the second cold flow from the second heat exchanger 9
The final temperature of the cold fluid that body entrance 93 enters is main by the 11 pairs of gas after third time gas-liquid separation is processed of choke valve
Part obtains after carrying out the temperature reduction caused in step-down processing procedure, therefore for by after third time gas-liquid separation treatment
The air pressure of gas part has certain requirement, and then has to the air pressure of the tail gas after the compression treatment of compressor 3 certain
It is required that.Therefore can effectively be run in order that obtaining whole system, in the present invention, it is preferred to set by after the compression of compressor 3 treatment
The air pressure of tail gas be not less than 0.5MPa.A.
In addition, it is 30 DEG C~50 further preferably to be set in the present invention by the temperature of the tail gas after first time cooling treatment
℃.The benefit for so setting is that the exhaust temperature after first time cooling is processed can be made to be down to normal temperature or so, then by the tail
Gas is in the nitrogen gas liter to be recycled by that will can enter from the first cold fluid inlet 63 after the heat exchange cooling of First Heat Exchanger 6
Temperature to close to normal temperature, in order to direct recovery and utilization subsequently to nitrogen.More specifically, at above-mentioned process first time cooling
In the case that the temperature of the tail gas after reason is 30 DEG C~50 DEG C, the present invention further preferably sets and is carried out by First Heat Exchanger 6
The temperature of the gas after second cooling treatment is -30 DEG C~-5 DEG C.
In addition, in the case of the corresponding air pressure of above-mentioned setting, temperature, the present invention can effectively enter in order that obtaining subsequent treatment
OK, the gas after First Heat Exchanger 6 carries out cooling treatment is further carried out at third time cooling by the second cooler 7
Reason, and third time cooling is processed as pressure cooling treatment, that is, need to carry out cooling treatment by being additionally provided the energy, such as adopts
Cooling treatment is carried out with refrigeration machine.Specifically, the present invention is preferably provided with by after the third time cooling treatment of the second cooler 7
The temperature of gas is -50 DEG C~-35 DEG C.
By to carrying out second gas-liquid separation treatment by the gas after third time cooling treatment, changed by second again afterwards
Gas part after the 9 pairs of separation of hot device carries out heat exchange cooling treatment again, with further by the reduction of its temperature.Specifically, this
The temperature that invention is preferably provided with the gas after the 4th cooling is processed is -80 DEG C~-65 DEG C.So set benefit be,
On the one hand can ensure that tetrahydrofuran or ethyl acetate are always liquid without solidifying, and then ensure having for later stage gas-liquid separator
Effect is separated, and on the other hand can ensure that the purity of the nitrogen of final recovery is higher.
The exemplary embodiments that the technique of nitrogen is reclaimed in a kind of tail gas from vacuum drying oven described in the invention described above are as follows：
After entering the buffered of surge tank 2 from the tail gas of vacuum drying oven discharge, it is compressed to by compressor 3 and improves air pressure
To 0.6MPa.A, the temperature of the gas after compression is reduced near normal temperature by the first cooler 4 then, such as 45 DEG C；It is laggard
Enter in the first gas-liquid separator 5 to carry out the gas-liquid separation of first time；Enter by the gas part after first time gas-liquid separation
- 20 DEG C are cooled in First Heat Exchanger 6, then -35 DEG C is further cooled to by the second cooler 7 again；Then again will
Being entered into the second gas-liquid separator 8 through the gas after above-mentioned cooling carries out secondary gas-liquid separation；By second gas-liquid
Then gas part after separation enters back into in the 3rd gas-liquid separator into being cooled to -65 DEG C in the second heat exchanger 9
The gas-liquid separation of row third time；Nitrogen is mainly by the gas part after third time gas-liquid separation, i.e., the nitrogen for utilizing to be recycled
Gas, now substantially -65 DEG C of its temperature, pressure substantially 0.6MPa.A；Afterwards again by by the gas after third time gas-liquid separation
Body portion is throttled to close to normal pressure 140kPa.A by choke valve 11, and causes its gas temperature to be further reduced to therewith
About -68 DEG C；Then the gas that temperature after step-down is about -68 DEG C is further passed sequentially through into the second heat exchanger 9 and first
It is warming up to after heat exchanger 6 close to about 30 DEG C of normal temperature, so by as low-temperature receiver and passing sequentially through the second heat exchanger 9 and
One heat exchanger 6 can make full use of the cold energy of the portion gas, reach maximally utilizing for efficiency.And by the first gas-liquid separator
5th, the second gas-liquid separator 8 and the separated liquid portion out of the 3rd gas-liquid separator 10, then can be converged by sewer pipe 12
Flow and be collected.
In addition, the barometric millimeter of mercury kPa.A and MPa.A that are used in the invention described above, be referred to as respectively absolute pressure kPa and
MPa, illustrates hereby.
Certainly, without loss of generality, heretofore described system and technique that nitrogen is reclaimed from vacuum drying oven tail gas, when
When what is contained in vacuum drying oven tail gas is other protective gas in addition to nitrogen, when such as certain inert gas, in theory
Also the inert gas in the tail gas can be recycled using system of the present invention and technique, for example, works as vacuum drying oven
Replace the situation of nitrogen in tail gas for argon gas.
Claims (10)
1. the system that nitrogen is reclaimed in a kind of tail gas from vacuum drying oven, it is characterised in that：Including
Surge tank (2), the surge tank (2) connects with the tail gas outlet of vacuum drying oven (1)；
Compressor (3), the entrance of the compressor (3) is connected with surge tank (2)；
First cooler (4), the entrance of first cooler (4) and the outlet of compressor (3)；
First gas-liquid separator (5), the entrance of first gas-liquid separator (5) and the outlet of the first cooler (4)；
First Heat Exchanger (6), is provided with the first thermal fluid inlet (61), the first hot fluid outlet ports on First Heat Exchanger (6)
(62), the first cold fluid inlet (63) and the first cold fluid outlet (64)；First thermal fluid inlet (61) and the first gas-liquid
Gas vent connection on separator (5)；
Second cooler (7), the entrance of second cooler (7) is connected with the first hot fluid outlet ports (62)；
Second gas-liquid separator (8), the entrance of second gas-liquid separator (8) and the outlet of the second cooler (7)；
Second heat exchanger (9), is provided with the second thermal fluid inlet (91), the second hot fluid outlet ports on the second heat exchanger (9)
(92), the second cold fluid inlet (93) and the second cold fluid outlet (94)；Second thermal fluid inlet (91) and the second gas-liquid
Gas vent connection on separator (8)；
3rd gas-liquid separator (10), the entrance of the 3rd gas-liquid separator (10) is connected with the second hot fluid outlet ports (92)；
And the gas vent on the 3rd gas-liquid separator (10) is connected with the second cold fluid inlet (93)；
Choke valve (11), one end of the choke valve (11) connects with the second cold fluid outlet (94), choke valve (11) it is another
End connects with first cold fluid inlet (63)；
First cold fluid outlet (64) is nitrogen recycling port.
2. the system for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 1, it is characterised in that：In the first gas-liquid point
Bottom from device (5), the second gas-liquid separator (8) and the 3rd gas-liquid separator (10) three is respectively arranged with waste liquid outlet, and
And the waste liquid outlet is connected with sewer pipe (12) respectively.
3. the system for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 1, it is characterised in that：First heat exchange
Device (6) and the second heat exchanger (9) are plate-fin heat exchanger.
4. the system that nitrogen is reclaimed from vacuum drying oven tail gas as described in any one in claims 1 to 3, its feature exists
In：First cooler (4) is air cooler or water cooling heat exchanger, and second cooler (7) is refrigeration machine.
5. the technique that nitrogen is reclaimed in a kind of tail gas from vacuum drying oven, using described in any one in the claims 1 to 4
The system that nitrogen is reclaimed from vacuum drying oven tail gas, for from the vacuum drying oven tail gas containing tetrahydrofuran and/or ethyl acetate
Middle recovery nitrogen, it is characterised in that：Comprise the following steps：
A. the tail gas discharged from the tail gas outlet of vacuum drying oven (1) obtains buffered in surge tank (2) first；
B. enter compressor (3) by the tail gas after buffered and processed by compression；
C. the tail gas after being processed through overcompression enters the first cooler (4) and is processed by first time cooling；
D. enter the first gas-liquid separator (5) by the tail gas after first time cooling treatment and processed by first time gas-liquid separation；
E. First Heat Exchanger (6) is entered and by second cooling treatment by the gas part after first time gas-liquid separation treatment；
F. enter the second cooler (7) by the gas after second cooling treatment and processed by third time cooling；
G. the second gas-liquid separator (8) is entered and by second gas-liquid separation treatment by the gas after third time cooling treatment；
H. the second heat exchanger (9) is entered and by the 4th cooling treatment by the gas part after second gas-liquid separation treatment；
I. enter the 3rd gas-liquid separator (10) by the gas after the 4th cooling treatment and processed by third time gas-liquid separation；
J. by third time gas-liquid separation treatment after gas part enter choke valve (11) and be depressurized to 110kPa.A~
250kPa.A, while by the 5th cooling treatment；
K. the second heat exchanger (9) is entered and by first time hyperthermic treatment by the gas of choke valve (11)；
L. First Heat Exchanger (6) is entered and by second hyperthermic treatment by the gas after first time hyperthermic treatment, by second
Gas after secondary hyperthermic treatment is discharged from nitrogen recycling port.
6. the technique for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 5, it is characterised in that：By compressor
(3) air pressure of the tail gas after compression treatment is not less than 0.5MPa.A.
7. the technique for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 6, it is characterised in that：Dropped by first time
The temperature of the tail gas after temperature treatment is 30 DEG C~50 DEG C.
8. the technique for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 7, it is characterised in that：Dropped by second
The temperature of the gas after temperature treatment is -30 DEG C~-5 DEG C.
9. the technique for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 8, it is characterised in that：Dropped by third time
The temperature of the gas after temperature treatment is -50 DEG C~-35 DEG C.
10. the technique for reclaiming nitrogen from vacuum drying oven tail gas as claimed in claim 9, it is characterised in that：By the 4th time
The temperature of the gas after cooling treatment is -80 DEG C~-65 DEG C.
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| CN102198337A (en) * | 2010-03-22 | 2011-09-28 | 杨峥雄 | Environment-friendly energy-saving exhaust gas treatment device and method |
| CN202892961U (en) * | 2012-10-24 | 2013-04-24 | 浙江鸿基石化有限公司 | Recovery device for tail gas generated in polypropylene production process |
| WO2015148927A1 (en) * | 2014-03-28 | 2015-10-01 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for separating no2 from a co2 and no2-containing fluid |
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