CN106196885A - A kind of air separation unit automatic energy-saving operation process - Google Patents
A kind of air separation unit automatic energy-saving operation process Download PDFInfo
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- CN106196885A CN106196885A CN201610525323.1A CN201610525323A CN106196885A CN 106196885 A CN106196885 A CN 106196885A CN 201610525323 A CN201610525323 A CN 201610525323A CN 106196885 A CN106196885 A CN 106196885A
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- nitrogen
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- separation unit
- cold blowing
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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
- F25J3/02—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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
- F25J3/02—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
- F25J3/04—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 for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
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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
- F25J3/02—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
- F25J3/04—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 for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention belongs to spatial division technology field, particularly to a kind of air separation unit automatic energy-saving operation process, the air after compression initially enters purification system and removes CO2And moisture, enter through air after purification and after distillation system carries out rectification, obtain nitrogen, oxygen and dirty nitrogen, its tolerance is that 16000 20000Nm/h sends into heater heating 1.5h after being computed regulating system-computed by dirty nitrogen, is to send into purification system after 16000 20000Nm/h sends into heater heating 1.5h to realize the heat treated of regeneration gas process by dirty nitrogen amount；Heat treated is complete, then according to actual condition, cold blowing dirt nitrogen feeding purification system will be completed regeneration gas cold blowing and process；Cold blowing amount and the cold blowing time of described dirty nitrogen process according to actual condition；The purification system energy consumption of air separation unit is reasonably preferably minimized and sends distillation system portioned product outside and makes adjustment in time by the present invention, to reach the energy-saving and cost-reducing of air separation unit.
Description
Technical field
The invention belongs to spatial division technology field, particularly to a kind of air separation unit automatic energy-saving operation process.
Background technology
Along with country's reinforcement to energy-saving and emission-reduction dynamics, Chemical Manufacture industry increasingly payes attention to the reduction of energy consumption, special
It is not Air separation industry, more than the 90% of total energy consumption is accounted for for its power consumption from the point of view of air separation unit, how to reduce power consumption and become empty
Separating device reduces the key of cost.The main power consumption of air separation unit is air compression system and purification system at present, due to space division
Unit scale is increasing, therefore its press can only use centrifugal compressor, and therefore its reducing energy consumption is less.Purification system becomes
Starting with a little for reducing energy consumption, traditional purification system utilizes molecular sieve and aluminium oxide to the water in air, carbon dioxide and second
Alkynes adsorbs, and needs to utilize dirty nitrogen to regenerate after absorption is saturated, and regeneration is broadly divided into heating and cold blowing.In heating
Time, dirty nitrogen heated by electric heater, and during cold blowing, electric heater cuts out, and the electricity the most typically used due to air-treatment amount adds
Hot device power is the biggest.And when design, be set when the service data of purification system is according to full production, but
Air separation unit does not often reach full production, has now resulted in the energy waste of air separation unit.
Therefore, it is necessary to provide a kind of air separation unit energy-saving run technique, can be automatically adjusted simultaneously and solve
State problem.
Summary of the invention
It is an object of the invention to provide a kind of air separation unit automatic energy-saving operation process, reasonably pure by air separation unit
Change system energy consumption is preferably minimized and sends distillation system portioned product outside makes adjustment, in time to reach the joint of air separation unit
Can consumption reduction.
A kind of air separation unit automatic energy-saving operation process: the air after compression initially enters purification system and removes CO2With
Moisture, needs to adjust the cycle of operation of purification system according to compressed-air actuated air inflow during this；Then will be through after purification
Air enter after distillation system carries out rectification obtain nitrogen that bulk purity is 99.99%, bulk purity is the oxygen of 99.6%
With the dirty nitrogen that nitrogen bulk purity is 94%, nitrogen is sent to user after entering nitrogen pressure compression system；Oxygen can be routed directly to use
Family；After dirty nitrogen is computed regulating system-computed, it is that 16000-20000Nm/h sends into heater heating 1.5h by dirt nitrogen amount
Rear feeding purification system realizes the heat treated of regeneration gas process, is then discharged by the residue dirt nitrogen produced in heating process；
Heat treated is complete, then according to actual condition, cold blowing dirt nitrogen feeding purification system will be completed regeneration gas cold blowing and process；Institute
Cold blowing amount and the cold blowing time of the dirty nitrogen stated process according to actual condition；The residue dirt nitrogen that finally will produce during cold blowing
Chilldown system can be sent into recirculated water is lowered the temperature；
Heretofore described purification system, uses 13X molecular sieve and alumina bed to carry out pressure-variable adsorption, is used for adsorbing dioxy
Change carbon, water, and regeneration gas can be utilized to regenerate；Described distillation system, is used for air cooling and carries out rectification
To produce oxygen, nitrogen and dirty nitrogen；Described calculating regulation system, enters described purification system air capacity for basis and carries out
Calculate with adjusting process flow process, to realize energy-conservation adjustment operation；Described heater, intermittence is operated to realize purification
System regeneration stepwise heating and the control of cold blowing；
Through look into different pressures, at a temperature of the aqueous scale of saturated moist air understand:
Under 0.5MPa (g) pressure, when temperature is 10 DEG C, compressed air saturation moisture content is 9.35g/m；
Under 0.5MPa (g) pressure, when temperature is 12 DEG C, compressed air saturation moisture content is 10.721g/m；
Contained CO in air2Content is generally 300-400ppm, takes CO in the present invention in air2Content is 350ppm.
Under nominal situation, purification system cycle of operation is 4h, and the reckoning process of its adsorbance is as follows:
When air separation unit is properly functioning, pressure is generally 0.46-0.49MPa (g), and according at identical temperature, it is empty that pressure gets over low compression
Saturation moisture content in gas is the highest, when therefore air separation unit is properly functioning its enter tower compressed air pressure use 0.5Mpa (g) enter
Row Conservative estimation.
When air separation unit is properly functioning, it enters tower compressed air (going out purification system) pressure is 0.5MPa (g) 601KPa
(A), temperature is 12 DEG C, and flow is 78000Nm/h, and according to The Ideal-Gas Equation PV=nRT, standard pressure takes 101KPa,
According to P in fact ' V is real '=PReasonVReason,Wherein P is real '=601KPa(A), PReason=101KPa(A), VReason=78000Nm³/h；
Obtaining actual volume is: V reality=78000*101/601=13108m/h；
If at the beginning of before entering molecular sieve, flow is V, according to V just '-VCO2'-V water '=V reality '；
V just-0.035%V just-10.721V just * RT/MP=V is real；
Wherein R=8.314KJ/ (mol*K) T=285K M=18g/mol P=6.01*106 PA
0.035% is CO in air2Content；10.721 is 0.5MPa (g), compressed air saturation moisture content when 12 DEG C；
Be computed V just=13143m/h；
Then purification system CO absorption per hour2Amount is: VCO2At the beginning of=0.035%*V=4.6m/h
CO under mark condition2Density is 1.96Kg/m, therefore its CO absorption per hour2Quality is
mCO2=4.6*601/101*1.96=53.65Kg/h；
The purification system operation time is 4 hours at present, the most co-adsorption CO2Quality is 214.6Kg；
Adsorpting water quantity is m per hourH2O=13143*10.721/1000=140.9kg/h；
4 hours co-adsorption water yields are 140.9*4=563.6 Kg；
To sum up result of calculation understands purification system the most each adsorption cycle CO absorption2Amount is 214.6Kg, adsorbs water
Amount is 563.6 Kg.
Under actual condition, purification system cycle of operation calculates that process is as follows:
With the air inflow of air separation unit compressed gas as 60000-61000Nm/h, pressure is 0.46Mpa(g) i.e. 561KPa(A),
Temperature is to calculate as a example by the operating mode of 10 DEG C, then be that 60500Nm/h calculates according to air separation unit air inflow:
According to P in fact ' V is real '=PReasonVReason,Wherein P is real '=561KPa(A), PReason=101KPa(A), VReason=60500Nm³/h；
Real gas volume is that V is real '=60500*101/561=10892m/h；
If flow is that V is first before entering molecular sieve ', according to V just '-VCO2'-V water '=V reality '；
V is just '-0.035%V just '-9.35V is just ' * RT/MP=V real '
Wherein R=8.314KJ/ (mol*K) T=283K
M=18g/mol P=5.61*106 PA
9.35 is at 0.5MPa (g), compressed air saturation moisture content when 10 DEG C；
Be computed V just '=10919m/h；
Then purification system CO absorption per hour2Amount is:
VCO2'=0.035%*V is just '=3.82m/h；
CO under mark condition2Density is 1.96Kg/m, therefore its CO absorption per hour2Quality is
mCO2’=3.82*561/101*1.96=41.59Kg/h；
Adsorpting water quantity is m per hourH2O=10919*9.35/1000=102.1kg/h(9.35 is at 0.5MPa (g), presses when 10 DEG C
Contracting saturation of the air water content, 1000 is mass conversion)；
When running according to normal duty, purification system can be with CO absorption2Amount is 214.6kg, then CO after load down produces2Absorption reaches
It is 214.6/41.59=5.16h to this value adsorption time；
When water is adsorbed onto 563.6 Kg, the operation time is 563.6/102.1=5.52h；
Compare through calculating, according to CO2Adsorption time increments 1.16h value, then molecular sieve cycle of operation can increase about
1h。
The reckoning process of cold blowing dirt nitrogen quantity and cold blowing time under actual condition:
Calculate as a example by below air separation unit purification system primary operating parameter:
Purification system normal working temperature 10 DEG C (283K)；During heating, dirt nitrogen inlet temperature is 161 DEG C (434K), and outlet temperature is
30 DEG C (303K), its dirty nitrogen temperature rise is 368.5K(inlet temperature and outlet temperature meansigma methods)；Nitrogen temperature 12 DEG C during cold blowing
(285K) when at the end of, during 20 DEG C of (293K) cold blowings of outlet temperature, nitrogen temperature is 363.5K(heating when dirt nitrogen inlet and cold blowing
Dirty nitrogen outlet mean temperature).
During cold blowing, dirty nitrogen needs the sensible heat by cylinder, molecular sieve and aluminium oxide to take away, therefore three when needing to calculate heating
Sensible heat.
Separate unit purification system quality is 3590Kg, and the specific heat of ferrum is 0.5KJ/ (Kg k);Every purification system fills 13X
Molecular sieve amount is 21T, aluminium oxide be 6.5T, 13X molecular sieve specific heat be 0.88KJ/ (Kg k), aluminium oxide specific heat is 0.78KJ/
(Kg·k)；Dirty nitrogen specific heat is 1.044KJ/ (Kg k).
According to Q=Δ t*m*C；Specific heat capacity is C, and quality is m, and Δ t is temperature difference；
Then cylinder sensible heat is Q1=3590*0.5*(368.5-283)=1.53*105KJ；
Molecular sieve and aluminium oxide sensible heat Q2=0.88*21000*(368.5-283)+0.78*6500*(368.5-283)=2.013*
106KJ；
Therefore dirt nitrogen needs the heat Q=Q1+Q2=2.166*10 taken away altogether during cold blowing6KJ；
During cold blowing, purification system is down to 293K from 368.5K, and its mean temperature is 330.75K；
The density of dirty nitrogen is 1.357kg/ m；
The heat that then every 1m dirt nitrogen is absorbed when being warming up to 330.75K by 285K is
Q=1.357*1.044*(330.75-285)=64.81 KJ/m；
The cold blowing time of current 2 hours then needs cold blowing dirt nitrogen quantity theory to be V=(2.166*106/ 64.81)/2=16719m/h；
If being become the cold blowing time 3 hours, cold blowing dirt nitrogen theoretical amount is 11140m/h.
The calculating process of the dirty nitrogen quantity of residue during cold blowing:
Dirty nitrogen quantity=the device of residue produces dirty nitrogen quantity-cold blowing dirt nitrogen amount
Based on above-mentioned calculation, carry out calculating the design of regulation system, for ensureing the stability of space division operating mode, use
Air inflow interval is adjusted, and regulation tolerance interval is respectively 40000-45000Nm/h, 45000-50000Nm/h, 50000-
55000Nm/h, 55000-60000Nm/h, 60000-70000Nm/h, 70000-80000Nm/h, according to compressed gas
Air inflow adjusts the cycle of operation of purification system, and adjusts cold blowing dirt nitrogen quantity and cold blowing time according to actual condition, to realize sky
The energy-conservation purpose of separating device purification system.
Beneficial effects of the present invention: can accomplish that air separation unit automatic energy-saving runs by actual production operating mode, saves energy
Source, practical, greatly reduce production cost.
Accompanying drawing explanation
Fig. 1 is air separation unit automatic energy-saving operation process schematic flow sheet of the present invention.
Detailed description of the invention
Embodiment 1
The present embodiment enters tower tolerance with 60000-61000Nm/h at air separation unit, and pressure is 0.46Mpa(g) i.e. 561KPa(A),
As a example by temperature is 10 DEG C, wherein air separation unit enters tower tolerance and then calculates according to 60500Nm/h:
Air after compression enters purification system with 60500Nm/h air inflow and removes CO2And moisture, CO absorption2Quality is
41.59Kg/h, the quality of absorption water is 102.1Kg/h, and the cycle of operation needing purification system is 5.16h；Then will be through pure
Air after change enter obtain nitrogen that bulk purity is 99.99% after distillation system carries out rectification, bulk purity is 99.6%
Oxygen and nitrogen bulk purity are the dirty nitrogen of 94%, and nitrogen is sent to user after entering nitrogen pressure compression system；Oxygen can be routed directly to
User；After dirty nitrogen is computed regulating system-computed, it is that 16000-20000Nm/h sends into heater heating by dirt nitrogen amount
Send into purification system after 1.5h and realize the heat treated of regeneration gas process, the residue dirt nitrogen produced in heating process is discharged；
Heat treated is complete, then will process according to cold blowing dirt nitrogen feeding purification system is completed regeneration gas cold blowing, described dirty nitrogen
The cold blowing amount of gas is 11140m/h, and the cold blowing time is 3h；Residue dirt nitrogen quantity (the dirty nitrogen of residue that finally will produce during cold blowing
Amount=device produces dirty nitrogen quantity-cold blowing dirt nitrogen quantity) chilldown system can be sent into recirculated water is lowered the temperature.
Molecular sieve cycle of operation reckoning process:
According to P in fact ' V is real '=PReasonVReason,Wherein P is real '=561KPa(A), PReason=101KPa(A), VReason=60500Nm³/h；
Real gas volume is that V is real '=60500*101/561=10892m/h；
If flow is that V is first before entering molecular sieve ', according to V just '-VCO2'-V water '=V reality '；
V is just '-0.035%V just '-9.35V is just ' * RT/MP=V real '
Wherein R=8.314KJ/ (mol*K) T=283K
M=18g/mol P=5.61*106 PA
9.35 is at 0.5MPa (g), compressed air saturation moisture content when 10 DEG C；
Be computed V just '=10919m/h；
Then purification system CO absorption per hour2Amount is:
VCO2'=0.035%*V is just '=3.82m/h；
CO under mark condition2Density is 1.96Kg/m, therefore its CO absorption per hour2Quality is
mCO2’=3.82*561/101*1.96=41.59Kg/h；
Adsorpting water quantity is m per hourH2O=10919*9.35/1000=102.1kg/h(9.35 is at 0.5MPa (g), presses when 10 DEG C
Contracting saturation of the air water content, 1000 is mass conversion)；
When running according to normal duty, purification system can be with CO absorption2Amount is 214.6kg, then CO after load down produces2Absorption reaches
It is 214.6/41.59=5.16h to this value adsorption time；
When water is adsorbed onto 563.6 Kg, the operation time is 563.6/102.1=5.52h；
The cycle of operation of purification system can be 5.16h.
The reckoning process of cold blowing dirt nitrogen quantity and cold blowing time under this operating mode:
Air separation unit purification system primary operating parameter is as follows at present:
Purification system normal working temperature 10 DEG C (283K)；Nitrogen temperature 12 DEG C (285K) during cold blowing, at the end of outlet temperature 20
DEG C (293K), dirt nitrogen outlet mean temperature when dirt nitrogen inlet and cold blowing when nitrogen temperature is 363.5K(heating during cold blowing).
During cold blowing, dirty nitrogen needs the sensible heat by cylinder, molecular sieve and aluminium oxide to take away, therefore three when needing to calculate heating
Sensible heat.
Separate unit purification system quality is 3590Kg, and the specific heat of ferrum is 0.5KJ/ (Kg k);Every purification system fills 13X
Molecular sieve amount is 21T, aluminium oxide be 6.5T, 13X molecular sieve specific heat be 0.88KJ/ (Kg k), aluminium oxide specific heat is 0.78KJ/
(Kg·k)；Dirty nitrogen specific heat is 1.044KJ/ (Kg k).
According to Q=Δ t*m*C；Specific heat capacity is C, and quality is m, and Δ t is temperature difference；
Then cylinder sensible heat is Q1=3590*0.5*(368.5-283)=1.53*105KJ；
Molecular sieve and aluminium oxide sensible heat Q2=0.88*21000*(368.5-283)+0.78*6500*(368.5-283)=2.013*
106KJ；
Therefore dirt nitrogen needs the heat Q=Q1+Q2=2.166*10 taken away altogether during cold blowing6KJ；
During cold blowing, purification system is down to 293K from 368.5K, and its mean temperature is 330.75K；
The heat that every 1m dirt nitrogen is absorbed when being warming up to 330.75K by 285K is
Q=1.357*1.044*(330.75-285)=64.81 KJ/m；
The cold blowing time of current 3 hours then needs dirty nitrogen quantity theory to be V=(2.166*106/ 64.81)/3=11140m/h.
Claims (4)
1. an air separation unit automatic energy-saving operation process, it is characterised in that: the air after compression initially enters purification system
Remove CO2And moisture, need to adjust according to compressed-air actuated air inflow the cycle of operation of purification system during this；Then by pure
Air after change enters and obtains nitrogen, oxygen and dirty nitrogen after distillation system carries out rectification, and dirty nitrogen is computed regulation system meter
After calculation by its tolerance be 16000-20000Nm/h send into heater heating 1.5h, then by this heating dirt nitrogen send into purification system
System realizes the heat treated of regeneration gas process, is then discharged by the residue dirt nitrogen produced in heating process；Heat treated is complete,
Then according to actual condition, cold blowing dirt nitrogen feeding purification system will be completed regeneration gas cold blowing to process；Described dirty nitrogen cold
The amount of blowing and cold blowing time process according to actual condition.
2. air separation unit automatic energy-saving operation process as claimed in claim 1, it is characterised in that: the described sky after compression
The air inflow of gas is 40000-45000Nm/h, 45000-50000Nm/h, 50000-55000Nm/h, 55000-60000Nm
/ h, 60000-70000Nm/h, any one of 70000-80000Nm/h.
3. air separation unit automatic energy-saving operation process as claimed in claim 1, it is characterised in that: the volume of described nitrogen
Purity is 99.99%；The bulk purity of described oxygen is 99.6%；The bulk purity of described dirty nitrogen is 94%.
4. air separation unit automatic energy-saving operation process as claimed in claim 1, it is characterised in that: dirty nitrogen is meeting purification system
In system cold blowing processing procedure, dirty for residue nitrogen can be sent into chilldown system recirculated water is lowered the temperature.
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| CN111238167A (en) * | 2020-03-17 | 2020-06-05 | 北京科技大学 | Energy-saving heating device and method for air separation device |
| CN115282747A (en) * | 2022-08-03 | 2022-11-04 | 中国石油化工股份有限公司 | Emergency treatment method for purifier in air separation device |
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| CN115282747B (en) * | 2022-08-03 | 2024-02-13 | 中国石油化工股份有限公司 | Emergency treatment method for purifier in air separation device |
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Application publication date: 20161207 |