CN104654739B - The apparatus and method that food-class liquid CO 2 is produced using two-tower rectification purification - Google Patents
The apparatus and method that food-class liquid CO 2 is produced using two-tower rectification purification Download PDFInfo
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- CN104654739B CN104654739B CN201510068104.0A CN201510068104A CN104654739B CN 104654739 B CN104654739 B CN 104654739B CN 201510068104 A CN201510068104 A CN 201510068104A CN 104654739 B CN104654739 B CN 104654739B
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Abstract
The invention belongs to the apparatus and method that food-class liquid CO 2 is produced in a kind of utilization two-tower rectification purification；It is connected with the import of unstripped gas four-stage compressor including the outlet of air inlet surge tank, the outlet of unstripped gas four-stage compressor is connected with the raw material gas inlet of first rectifying column middle and lower part by the first reboiler, the liquid-phase outlet of first rectifying column bottom is connected with catcher, gaseous phase outlet at the top of first rectifying column is connected with the gas phase import of overhead condenser, the liquid-phase outlet of overhead condenser is connected with the fluid inlet on first rectifying column top, pipeline between the liquid-phase outlet of overhead condenser and the fluid inlet on first rectifying column top is provided with the first threeway, 3rd end of the first threeway is connected with inlet in the middle part of Second distillation column by pipeline；The liquid-phase outlet of Second distillation column bottom is connected with carbon dioxide storage tank by pipeline and the inlet of First Heat Exchanger, the liquid outlet of First Heat Exchanger；It is simple, easy to operate with technological process, the advantage of stable and low energy consumption.
Description
Technical field
The invention belongs to carbon dioxide production technical field, and in particular to a kind of to produce food stage using two-tower rectification purification
The apparatus and method of liquid CO 2.
Background technology
The production of traditional food grade carbon-dioxide typically adopt the de- hydrocarbon device of molecular sieve dehydration dealcoholysis and Production by Catalytic Combustion Process and
Its technique；Wherein, substantial amounts of heat is needed to be used for thermal regeneration gas in the molecular sieve dehydration dealcoholysis stage, energy consumption is higher, dehydration
Dealcoholysis then needs to sequentially pass through release, regeneration, cold blowing, presses, and operating process is complicated；The equipment of input is needed containing sequencing valve, suction
Attached dose, adsorption tower, electric heater etc. one-time investment is larger；The Production by Catalytic Combustion Process de- hydrocarbon stage using platinum, palladium series catalyst and
Patent equipment, price are higher, and its material needs to sequentially pass through preheating, heating, take off that hydrocarbon, water-cooled and ammonia are cold, and energy consumption is higher.Above-mentioned work
Skill process not only brings white elephant to manufacturing enterprise, is also to increased production cost using enterprise.
The content of the invention
It is an object of the invention to overcome defect of the prior art, and provide that a kind of flow process is simple, reasonable in design, operation
Food-class liquid CO 2 is produced in the utilization two-tower rectification purification of the low and disposable less investment of convenient, stable, energy consumption
Apparatus and method.
The object of the present invention is achieved like this：Including air inlet surge tank, the outlet of air inlet surge tank is by pipeline and raw material
The import of gas four-stage compressor is connected, and the outlet of unstripped gas four-stage compressor is by the first reboiler and first rectifying column middle and lower part
Raw material gas inlet be connected, the liquid-phase outlet of first rectifying column bottom is connected with catcher, and the gas phase at the top of first rectifying column goes out
Mouth is connected with the gas phase import of overhead condenser, and the liquid-phase outlet of overhead condenser is by pipeline and the liquid on first rectifying column top
Phase import is connected, and the pipeline between the liquid-phase outlet of overhead condenser and the fluid inlet on first rectifying column top is provided with first
Threeway, the 3rd end of the first threeway by pipeline successively with the second reboiler, feed liquor in the middle part of the first regulating valve and Second distillation column
Mouth is connected；The liquid-phase outlet of Second distillation column bottom is connected with the inlet of First Heat Exchanger by pipeline, First Heat Exchanger
Liquid outlet is connected with carbon dioxide storage tank；Gaseous phase outlet at the top of the overhead condenser passes through the second threeway and the second heat exchanger
Shell side be connected with gas-liquid separator, the liquid phase of the liquid-phase outlet of gas-liquid separator bottom by pipeline and Second distillation column top
Import is connected, and the gaseous phase outlet at the top of gas-liquid separator is connected with the first gas phase import of First Heat Exchanger, First Heat Exchanger
First gaseous phase outlet is connected with waste gas header；Gaseous phase outlet at the top of the Second distillation column passes through the of pipeline and the second threeway
Three ends are connected；Pipeline between second reboiler and the first regulating valve is provided with the 3rd threeway, and the of the 3rd threeway
Three ends pass through the second regulating valve and the tube side of the second heat exchanger is connected with the second gas phase import of First Heat Exchanger, First Heat Exchanger
The second gaseous phase outlet be connected with the two-stage compression air inlet of unstripped gas four-stage compressor by pipeline.
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank and unstripped gas four-stage compressor enters the first reboiler import, described
The component of unstripped gas is：Carbon dioxide 95～99%, water 0.4～2%, alcohol 0.1～2%, hydrocarbon 0.1～1%, temperature is：10～
40 DEG C, pressure is：0.1～0.2Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：90～120 DEG C,
Pressure is 4～6Mpa；
Step 2：Make smart by the first reboiler and first into the first reboiler imported materials gas described in step one
The raw material gas inlet for evaporating tower middle and lower part is entered in first rectifying column；The raw material gas inlet of the first rectifying column middle and lower part goes out raw material
Temperature degree is：30～80 DEG C；
Step 3：The unstripped gas entered in first rectifying column described in step 2 is made to pass through the first threeway with overhead condenser
Mass-and heat-transfer is carried out with the low-boiling point material in the fluid inlet on first rectifying column top into first rectifying column, after mass-and heat-transfer
High boiling substance it is condensed after entered in catcher by the liquid-phase outlet of first rectifying column bottom, its low-boiling point material passes through
The gas phase import of gaseous phase outlet and overhead condenser at the top of first rectifying column is entered in overhead condenser；The collection of the entrance
High boiling substance component in device is：Carbon dioxide 30～35%, alcohol 5～11%, water 40～60%, hydro carbons 0.1～1%, temperature
Spend and be：50～80 DEG C, pressure is 4～6Mpa；
Step 4：The liquid phase of low-boiling point material described in step 3 in overhead condenser is made by the first threeway, one
Enter in the fluid inlet on the liquid phase Jing first rectifying column top of point low-boiling point material in first rectifying column with first rectifying column in
Unstripped gas carry out mass-and heat-transfer, the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing, the 3rd
In the middle part of threeway, the first regulating valve and Second distillation column, inlet enters the inside of Second distillation column；Second the second reboiler of tunnel,
3rd threeway and the second regulating valve enter the tube side of the second heat exchanger；Low-boiling point material inside the entrance Second distillation column
Liquidus temperature is：5～-10 DEG C, pressure is 4～6Mpa, and flow is 748Nm3/h；Low boiling in the rectifying column tower top condenser
The liquid phase component of material：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are 5～-10 DEG C, and pressure is 4.8Mpa；Into
The liquidus temperature of the low-boiling point material of the second heat exchanger tube pass is：- 30～-45 DEG C, pressure is 1.0～2.0Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column described in step 4 and divided by gas-liquid
Enter into the carbon dioxide rich solution in Second distillation column from the liquid-phase outlet of device bottom and the fluid inlet on Second distillation column top
Row mass-and heat-transfer, after mass-and heat-transfer, the gas phase of secondary low-boiling point material discharges second by the gaseous phase outlet at the top of Second distillation column
Rectifying column, its secondary high boiling substance is by the liquid-phase outlet of Second distillation column bottom, the inlet of First Heat Exchanger and first
The liquid outlet of heat exchanger is entered in carbon dioxide storage tank；The secondary high boiling substance group of liquid-phase outlet of the Second distillation column bottom
It is divided into：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 10～-20 DEG C, pressure is 1.5～3.0Mpa；It is described
The temperature of the secondary high boiling substance of the inlet of First Heat Exchanger is：- 10～-20 DEG C, pressure is：1.5～3.0Mpa；It is described
The temperature of the secondary high boiling substance of liquid outlet of First Heat Exchanger is：- 15 DEG C～-20 DEG C, pressure is：1.5～3.0Mpa；It is described
Food-grade carbon-dioxide is into the secondary high boiling substance in carbon dioxide storage tank, its carbon dioxide content is 99.99%；
Step 6：The gas phase of the low-boiling point material described in step 3 in overhead condenser is made to pass through overhead condenser gas phase
Outlet and the second threeway are entered in the shell side of the second heat exchanger, make the secondary low boiling of Second distillation column is discharged described in step 5
The gas phase of material is entered by the second threeway in the shell side of the second heat exchanger, makes the gas phase and secondary low boilers of low-boiling point material
The gas phase of matter is entered in gas-liquid separator in the gas phase after mixed heat transfer in the shell side of the second heat exchanger；The overhead condenser gas
The gaseous component of the low-boiling point material for mutually exporting is carbon dioxide 50～65%, and temperature is：0～-10 DEG C, pressure is：4.8Mpa；
The gaseous component of the secondary low-boiling point material of the Second distillation column is：Carbon dioxide 91%, hydrogen 1%, oxygen 2.1%, nitrogen
Gas 5.9%, temperature is：0～-15 DEG C, pressure is 1.0～2.5Mpa；Gas in second heat exchanger shell pass after mixed heat transfer
Temperature is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator after mixed heat transfer is made to carry out gas-liquid separation, gas
Carbon dioxide rich solution after liquid is separated passes through the liquid-phase outlet of gas-liquid separator bottom and the fluid inlet on Second distillation column top
Into in Second distillation column, the waste gas after gas-liquid separation by the gaseous phase outlet at the top of gas-liquid separator, First Heat Exchanger the
First gaseous phase outlet of one gas phase import and First Heat Exchanger enters waste gas header；It is described go out gas-liquid separator bottom liquid phase go out
Mouthful carbon dioxide rich solution component be：Carbon dioxide 80～90%, temperature is：- 10～-32 DEG C, pressure is 1.5～3.0MPa；
It is described go out gas-liquid separator at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 30～52%, temperature are -10～-32 DEG C,
Pressure is 1.5～3.0MPa；
Step 8：The liquid phase of the low-boiling point material described in step 4 into the second heat exchanger tube pass is made to pass sequentially through second
Second gaseous phase outlet of heat exchanger tube pass, the second gas phase import of First Heat Exchanger and First Heat Exchanger enters unstripped gas level Four pressure
The two-stage compression air inlet of contracting machine；The liquid of the low-boiling point material of the two-stage compression air inlet of the entrance unstripped gas four-stage compressor
Phase temperature is：- 14 DEG C, pressure is 1.0～2.0Mpa.
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank and unstripped gas four-stage compressor enters the first reboiler import, described
The component of unstripped gas is：Carbon dioxide 98.1%, water 1%, alcohol 0.4%, hydrocarbon 0.5%, flow is：770Nm3/ h, temperature is：40
DEG C, pressure is：0.12Mpa；Temperature of the unstripped gas after unstripped gas four-stage compressor be：100 DEG C, pressure is
4.8Mpa；
Step 2：Make smart by the first reboiler and first into the first reboiler imported materials gas described in step one
The raw material gas inlet for evaporating tower middle and lower part is entered in first rectifying column；The raw material gas inlet of the first rectifying column middle and lower part goes out raw material
Temperature degree is：65℃；
Step 3：The unstripped gas entered in first rectifying column described in step 2 is made to pass through the first threeway with overhead condenser
Mass-and heat-transfer is carried out with the low-boiling point material in the fluid inlet on first rectifying column top into first rectifying column, after mass-and heat-transfer
High boiling substance it is condensed after entered in catcher by the liquid-phase outlet of first rectifying column bottom, its low-boiling point material passes through
The gas phase import of gaseous phase outlet and overhead condenser at the top of first rectifying column is entered in overhead condenser；The collection of the entrance
High boiling substance component in device is：Carbon dioxide 31.8%, alcohol 10.3%, water 57.8%, hydro carbons 0.1%, temperature is：69.4
DEG C, pressure is 4.8Mpa；
Step 4：The liquid phase of low-boiling point material described in step 3 in overhead condenser is made by the first threeway 13, one
Enter in the fluid inlet on the liquid phase Jing first rectifying column top of part low-boiling point material in first rectifying column and first rectifying column
In unstripped gas carry out mass-and heat-transfer, the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing,
In the middle part of three threeways, the first regulating valve and Second distillation column, inlet enters the inside of Second distillation column；Boil again on the second tunnel second
Device, the 3rd threeway and the second regulating valve enter the tube side of the second heat exchanger；Low boilers inside the entrance Second distillation column
The liquidus temperature of matter is：- 10 DEG C, pressure is 4.8Mpa, and flow is 748Nm3/h；Low boiling in the rectifying column tower top condenser
The liquid phase component of material：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are -5 DEG C, and pressure is 4.8Mpa；Into second
The liquidus temperature of the low-boiling point material of 6 tube side of heat exchanger is：- 34.5 DEG C, pressure is 1.26Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column described in step 4 and divided by gas-liquid
Enter into the carbon dioxide rich solution in Second distillation column from the liquid-phase outlet of 7 bottom of device and the fluid inlet on Second distillation column top
Row mass-and heat-transfer, after mass-and heat-transfer, the gas phase of secondary low-boiling point material discharges second by the gaseous phase outlet at the top of Second distillation column
Rectifying column, its secondary high boiling substance is by the liquid-phase outlet of Second distillation column bottom, the inlet of First Heat Exchanger and first
The liquid outlet of heat exchanger is entered in carbon dioxide storage tank；The secondary high boiling substance group of liquid-phase outlet of the Second distillation column bottom
It is divided into：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 12.1 DEG C, pressure is 2.5Mpa；First heat exchange
The temperature of the secondary high boiling substance of the inlet of device is：- 10～-20 DEG C, pressure is：2.5Mpa；The First Heat Exchanger
The temperature of the secondary high boiling substance of liquid outlet is：- 15 DEG C, pressure is：2.5Mpa；It is secondary in the entrance carbon dioxide storage tank
High boiling substance is food-grade carbon-dioxide, and its carbon dioxide content is 99.99%；
Step 6：The gas phase of the low-boiling point material described in step 3 in overhead condenser is made to pass through overhead condenser gas phase
Outlet and the second threeway are entered in the shell side of the second heat exchanger, make the secondary low boiling of Second distillation column is discharged described in step 5
The gas phase of material is entered by the second threeway in the shell side of the second heat exchanger, makes the gas phase and secondary low boilers of low-boiling point material
The gas phase of matter is entered in gas-liquid separator in the gas phase after mixed heat transfer in the shell side of the second heat exchanger；The overhead condenser gas
The gaseous component of the low-boiling point material for mutually exporting is carbon dioxide 63.1%, and temperature is：- 5 DEG C, pressure is：4.8Mpa；Described
The gaseous component of the secondary low-boiling point material of two rectifying columns is：Carbon dioxide 91%, hydrogen 1%, oxygen 2.1%, nitrogen
5.9%, temperature is：- 15.2 DEG C, pressure is 2.5Mpa；Gas temperature in second heat exchanger shell pass after mixed heat transfer
For：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator after mixed heat transfer is made to carry out gas-liquid separation, gas
Carbon dioxide rich solution after liquid is separated passes through the liquid-phase outlet of gas-liquid separator bottom and the fluid inlet on Second distillation column top
Into in Second distillation column, the waste gas after gas-liquid separation by the gaseous phase outlet at the top of gas-liquid separator, First Heat Exchanger the
First gaseous phase outlet of one gas phase import and First Heat Exchanger enters waste gas header；It is described go out gas-liquid separator bottom liquid phase go out
Mouthful carbon dioxide rich solution component be：Carbon dioxide 88.2%, temperature is：- 32 DEG C, pressure is 2.5MPa；It is described go out gas-liquid point
The waste gas component of the gaseous phase outlet at the top of device is：Carbon dioxide 43.8%, temperature are -32 DEG C, and pressure is 2.5MPa；
Step 8：The liquid phase of the low-boiling point material described in step 4 into the second heat exchanger tube pass is made to pass sequentially through second
Second gaseous phase outlet of heat exchanger tube pass, the second gas phase import of First Heat Exchanger and First Heat Exchanger enters unstripped gas level Four pressure
The two-stage compression air inlet of contracting machine；The liquid of the low-boiling point material of the two-stage compression air inlet of the entrance unstripped gas four-stage compressor
Phase temperature is：- 14 DEG C, pressure is 1.26Mpa.
With noble metal (Palladium molybdenums in traditional food grade carbon-dioxide production process) catalyst, as catalyst, is passed through oxygen, 425
Benzene, hydrocarbon compound are oxidized to into carbon dioxide and water under the conditions of DEG C, whole process palpus Jing electric heaters are heated to 425 DEG C.Urge
Change the gas after oxidation through cooling down again, after molecular sieve drying, cryogenic rectification is carried out into cryogenic system, remove oxygen etc. no
Food-grade carbon-dioxide is produced after solidifying property gas.The present invention overcomes above-mentioned traditional view using unstripped gas pressurizeing by compressor
To 4.8MPa, the unstripped gas after pressurization adjusts its temperature by the water-cooled of additional multiple line, is passed through the first of first rectifying column bottom
Reboiler, maintains rectifying column column bottom temperature between 50～75 DEG C by multiple line valve opening.From the first reboiler original out
Material gas is entered from the middle part of first rectifying column, and, from tower reactor discharge system, overhead condensation liquid partial reflux is most of cold for high boiling substance
Lime set body enters to the second reboiler of Second distillation column bottom and provides cold for rectification, is then divided into two strands, one throttling as
Second distillation column is entered after 3.5MPa, another meropodium flow to 1.2MPa and provides after cold into the first heat exchange for the second heat exchanger
Device, enters compressor secondary inlet after recovery section cold.Do not coagulate at the top of fixed gas and first rectifying column at the top of Second distillation column
The second heat exchanger shell pass is entered after gas bout, gas-liquid separator, in liquid-phase reflux to Second distillation column, gas after partial liquefaction, is entered
At the top of liquid/gas separator, fixed gas enters First Heat Exchanger, reclaims discharge system after cold；Second distillation column bottom high-purity dioxy
Change carbon supercool rear in carbon dioxide storage tank into First Heat Exchanger, it is simple, easy to operate with technological process, it is stable
With the advantage of low energy consumption.
Description of the drawings
Fig. 1 is the structural representation of the present invention.
Specific embodiment
As shown in figure 1, the present invention is to include air inlet surge tank 22, the outlet of air inlet surge tank 22 is by pipeline and unstripped gas four
The import of level compressor 1 is connected, and the outlet of unstripped gas four-stage compressor 1 is by the first reboiler 2 and 3 middle and lower part of first rectifying column
Raw material gas inlet be connected, the liquid-phase outlet of 3 bottom of first rectifying column is connected with catcher 4, the gas phase at the top of first rectifying column 3
Outlet is connected with the gas phase import of overhead condenser 5, and the liquid-phase outlet of overhead condenser 5 is by pipeline and first rectifying column 3
The fluid inlet in portion is connected, on the pipeline between the fluid inlet on 3 top of liquid-phase outlet and first rectifying column of overhead condenser 5
Be provided with the first threeway 13, the 3rd end of the first threeway 13 by pipeline successively with the second reboiler 8, the first regulating valve 10 and second
9 middle part inlet of rectifying column is connected；The liquid-phase outlet of 9 bottom of Second distillation column is by pipeline and the inlet of First Heat Exchanger 12
It is connected, the liquid outlet of First Heat Exchanger 12 is connected with carbon dioxide storage tank 16；Gaseous phase outlet at the top of the overhead condenser 5 leads to
The shell side for crossing the second threeway 14 and the second heat exchanger 6 is connected with gas-liquid separator 7, and the liquid-phase outlet of 7 bottom of gas-liquid separator leads to
Piping is connected with the fluid inlet on 9 top of Second distillation column, the gaseous phase outlet at the top of gas-liquid separator 7 and First Heat Exchanger 12
The first gas phase import 18 be connected, the first gaseous phase outlet 19 of First Heat Exchanger 12 is connected with waste gas header 17；Described second is smart
Evaporate the gaseous phase outlet at the top of tower 9 to be connected with the 3rd end of the second threeway 14 by pipeline；Second reboiler 8 and first is adjusted
Pipeline between valve 10 is provided with the 3rd threeway 15, and the 3rd end of the 3rd threeway 15 is changed by the second regulating valve 11 and second
The tube side of hot device 6 is connected with the second gas phase import 20 of First Heat Exchanger 12, and the second gaseous phase outlet 21 of First Heat Exchanger 12 leads to
Piping is connected with the two-stage compression air inlet of unstripped gas four-stage compressor 1.
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank 22 and unstripped gas four-stage compressor 1 enters 2 import of the first reboiler,
The component of the unstripped gas is：Carbon dioxide 95～99%, water 0.4～2%, alcohol 0.1～2%, hydrocarbon 0.1～1%, temperature is：
10～40 DEG C, pressure is：0.1～0.2Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：90～120
DEG C, pressure is 4～6Mpa；
Step 2：Make to enter 2 imported materials gas of the first reboiler described in step one by the first reboiler 2 and first
The raw material gas inlet of 3 middle and lower part of rectifying column is entered in first rectifying column 3；The raw material gas inlet of 3 middle and lower part of the first rectifying column
Going out unstripped gas temperature is：30～80 DEG C；
Step 3：The unstripped gas entered in first rectifying column 3 described in step 2 is made to pass through the one or three with overhead condenser 5
Logical 13 and 3 top of first rectifying column fluid inlet in enter the low-boiling point material of first rectifying column 3 and carry out mass-and heat-transfer, mass transfer
The condensed rear liquid-phase outlet for passing through 3 bottom of first rectifying column of high boiling substance after heat transfer is entered in catcher 4, its low boiling
Material is entered in overhead condenser 5 by the gas phase import of gaseous phase outlet and overhead condenser 5 at the top of first rectifying column 3；Institute
The high boiling substance component stated in the catcher 4 of entrance is：Carbon dioxide 30～35%, alcohol 5～11%, water 40～60%, hydrocarbon
Class 0.1～1%, temperature is：50～80 DEG C, pressure is 4～6Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser 5 described in step 3 is made by the first threeway 13, one
Enter in the fluid inlet on 3 top of liquid phase Jing first rectifying column of part low-boiling point material in first rectifying column 3 and the first rectification
Unstripped gas in tower 3 carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing
8th, the 3rd threeway 15, the first regulating valve 10 and 9 middle part inlet of Second distillation column enter the inside of Second distillation column 9；Second tunnel
Jing the second reboilers 8, the 3rd threeway 15 and the second regulating valve 11 enter the tube side of the second heat exchanger 6；It is described to enter the second rectification
The liquidus temperature of the low-boiling point material inside tower 9 is：5～-10 DEG C, pressure is 4～6Mpa, and flow is 748Nm3/h；The essence
Evaporate the liquid phase component of low-boiling point material in column overhead condenser 5：Carbon dioxide 99.3%, foreign gas 0.7%, temperature be 5～-
10 DEG C, pressure is 4.8Mpa；Liquidus temperature into the low-boiling point material of 6 tube side of the second heat exchanger is：- 30～-45 DEG C, pressure
For 1.0～2.0Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column 9 described in step 4 and pass through gas-liquid
The carbon dioxide that the fluid inlet on 9 top of liquid-phase outlet and Second distillation column of 7 bottom of separator is entered in Second distillation column 9 is rich
Liquid carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gaseous phase outlet row at the top of Second distillation column 9
Go out Second distillation column 9, its secondary high boiling substance is entered by the liquid-phase outlet of 9 bottom of Second distillation column, First Heat Exchanger 12
The liquid outlet of liquid mouth and First Heat Exchanger 12 is entered in carbon dioxide storage tank 16；The liquid-phase outlet of 9 bottom of the Second distillation column
Secondary high boiling substance component is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 10～-20 DEG C, pressure is
1.5～3.0Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger 12 is：- 10～-20 DEG C, pressure
For：1.5～3.0Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger 12 is：- 15 DEG C～-20 DEG C, pressure
Power is：1.5～3.0Mpa；Secondary high boiling substance in the entrance carbon dioxide storage tank 16 is food-grade carbon-dioxide,
Its carbon dioxide content is 99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser 5 described in step 3 is made to pass through 5 gas of overhead condenser
Mutually outlet and the second threeway 14 is entered in the shell side of the second heat exchanger 6, makes the secondary of Second distillation column 9 is discharged described in step 5
The gas phase of low-boiling point material is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase and two of low-boiling point material
The gas phase of secondary low-boiling point material is entered in gas-liquid separator 7 in the gas phase after mixed heat transfer in the shell side of the second heat exchanger 6；It is described
The gaseous component of the low-boiling point material of 5 gaseous phase outlet of overhead condenser is carbon dioxide 50～65%, and temperature is：0～-10 DEG C,
Pressure is：4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column 9 is：Carbon dioxide 91%, hydrogen
1%, oxygen 2.1%, nitrogen 5.9%, temperature is：0～-15 DEG C, pressure is 1.0～2.5Mpa；Second heat exchanger, 6 shell side
Gas temperature after interior mixed heat transfer is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer is made to carry out gas-liquid separation, gas
The liquid phase on liquid-phase outlet and Second distillation column 9 top of the carbon dioxide rich solution after liquid separation by 7 bottom of gas-liquid separator is entered
Mouth is entered in Second distillation column 9, and the waste gas after gas-liquid separation is by the gaseous phase outlet at the top of gas-liquid separator 7, First Heat Exchanger
12 the first gas phase import 18 and the first gaseous phase outlet 19 of First Heat Exchanger 12 enter waste gas header 17；It is described go out gas-liquid separation
The carbon dioxide rich solution component of the liquid-phase outlet of 7 bottom of device is：Carbon dioxide 80～90%, temperature is：- 10～-32 DEG C, pressure
For 1.5～3.0MPa；It is described go out gas-liquid separator 7 at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 30～52%, temperature
Spend for -10～-32 DEG C, pressure is 1.5～3.0MPa；
Step 8：The liquid phase described in step 4 into the low-boiling point material of 6 tube side of the second heat exchanger is made to pass sequentially through the
Second gaseous phase outlet 21 of two heat exchangers, 6 tube side, the second gas phase import 20 of First Heat Exchanger 12 and First Heat Exchanger 12 is entered
The two-stage compression air inlet of unstripped gas four-stage compressor 1；The two-stage compression air inlet of the entrance unstripped gas four-stage compressor 1
The liquidus temperature of low-boiling point material is：- 14 DEG C, pressure is 1.0～2.0Mpa.
The present invention is further described in conjunction with specific embodiment.Specific embodiment is as follows：
Embodiment one
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank 22 and unstripped gas four-stage compressor 1 enters 2 import of the first reboiler,
The component of the unstripped gas is：Carbon dioxide 95%, water 2%, alcohol 2%, hydrocarbon 1%, temperature is：10 DEG C, pressure is：0.1Mpa；
The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：90 DEG C, pressure is 4Mpa；
Step 2：Make to enter 2 imported materials gas of the first reboiler described in step one by the first reboiler 2 and first
The raw material gas inlet of 3 middle and lower part of rectifying column is entered in first rectifying column 3；The raw material gas inlet of 3 middle and lower part of the first rectifying column
Going out unstripped gas temperature is：30℃；
Step 3：The unstripped gas entered in first rectifying column 3 described in step 2 is made to pass through the one or three with overhead condenser 5
Logical 13 and 3 top of first rectifying column fluid inlet in enter the low-boiling point material of first rectifying column 3 and carry out mass-and heat-transfer, mass transfer
The condensed rear liquid-phase outlet for passing through 3 bottom of first rectifying column of high boiling substance after heat transfer is entered in catcher 4, its low boiling
Material is entered in overhead condenser 5 by the gas phase import of gaseous phase outlet and overhead condenser 5 at the top of first rectifying column 3；Institute
The high boiling substance component stated in the catcher 4 of entrance is：Carbon dioxide 30%, alcohol 10.5%, water 59%, hydro carbons 0.5%, temperature
Spend and be：50 DEG C, pressure is 4Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser 5 described in step 3 is made by the first threeway 13, one
Enter in the fluid inlet on 3 top of liquid phase Jing first rectifying column of part low-boiling point material in first rectifying column 3 and the first rectification
Unstripped gas in tower 3 carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing
8th, the 3rd threeway 15, the first regulating valve 10 and 9 middle part inlet of Second distillation column enter the inside of Second distillation column 9；Second tunnel
Jing the second reboilers 8, the 3rd threeway 15 and the second regulating valve 11 enter the tube side of the second heat exchanger 6；It is described to enter the second rectification
The liquidus temperature of the low-boiling point material inside tower 9 is：- 10 DEG C, pressure is 4Mpa, and flow is 748Nm3/h；The rectifying tower
The liquid phase component of low-boiling point material in the condenser 5 of top：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are -10 DEG C, pressure
For 4.8Mpa；Liquidus temperature into the low-boiling point material of 6 tube side of the second heat exchanger is：- 45 DEG C, pressure is 1.0Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column 9 described in step 4 and pass through gas-liquid
The carbon dioxide that the fluid inlet on 9 top of liquid-phase outlet and Second distillation column of 7 bottom of separator is entered in Second distillation column 9 is rich
Liquid carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gaseous phase outlet row at the top of Second distillation column 9
Go out Second distillation column 9, its secondary high boiling substance is entered by the liquid-phase outlet of 9 bottom of Second distillation column, First Heat Exchanger 12
The liquid outlet of liquid mouth and First Heat Exchanger 12 is entered in carbon dioxide storage tank 16；The liquid-phase outlet of 9 bottom of the Second distillation column
Secondary high boiling substance component is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 20 DEG C, pressure is
1.5Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger 12 is：- 10～-20 DEG C, pressure is：
1.5Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger 12 is：- 15 DEG C, pressure is：1.5Mpa；Institute
State into the secondary high boiling substance in carbon dioxide storage tank 16 and be food-grade carbon-dioxide, its carbon dioxide content is
99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser 5 described in step 3 is made to pass through 5 gas of overhead condenser
Mutually outlet and the second threeway 14 is entered in the shell side of the second heat exchanger 6, makes the secondary of Second distillation column 9 is discharged described in step 5
The gas phase of low-boiling point material is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase and two of low-boiling point material
The gas phase of secondary low-boiling point material is entered in gas-liquid separator 7 in the gas phase after mixed heat transfer in the shell side of the second heat exchanger 6；It is described
The gaseous component of the low-boiling point material of 5 gaseous phase outlet of overhead condenser is carbon dioxide 50%, and temperature is：- 10 DEG C, pressure is：
4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column 9 is：Carbon dioxide 91%, hydrogen 1%, oxygen
2.1%, nitrogen 5.9%, temperature is：- 15 DEG C, pressure is 1.0Mpa；Gas in second heat exchanger, 6 shell side after mixed heat transfer
Temperature is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer is made to carry out gas-liquid separation, gas
The liquid phase on liquid-phase outlet and Second distillation column 9 top of the carbon dioxide rich solution after liquid separation by 7 bottom of gas-liquid separator is entered
Mouth is entered in Second distillation column 9, and the waste gas after gas-liquid separation is by the gaseous phase outlet at the top of gas-liquid separator 7, First Heat Exchanger
12 the first gas phase import 18 and the first gaseous phase outlet 19 of First Heat Exchanger 12 enter waste gas header 17；It is described go out gas-liquid separation
The carbon dioxide rich solution component of the liquid-phase outlet of 7 bottom of device is：Carbon dioxide 80%, temperature is：- 32 DEG C, pressure is 1.5MPa；
It is described go out gas-liquid separator 7 at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 30%, temperature are -32 DEG C, and pressure is
1.5MPa；
Step 8：The liquid phase described in step 4 into the low-boiling point material of 6 tube side of the second heat exchanger is made to pass sequentially through the
Second gaseous phase outlet 21 of two heat exchangers, 6 tube side, the second gas phase import 20 of First Heat Exchanger 12 and First Heat Exchanger 12 is entered
The two-stage compression air inlet of unstripped gas four-stage compressor 1；The two-stage compression air inlet of the entrance unstripped gas four-stage compressor 1
The liquidus temperature of low-boiling point material is：- 14 DEG C, pressure is 1.0Mpa.
Embodiment two
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank 22 and unstripped gas four-stage compressor 1 enters 2 import of the first reboiler,
The component of the unstripped gas is：Carbon dioxide 99%, water 0.4%, alcohol 0.5%, hydrocarbon 0.1%, temperature is：40 DEG C, pressure is：
0.2Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：120 DEG C, pressure is 6Mpa；
Step 2：Make to enter 2 imported materials gas of the first reboiler described in step one by the first reboiler 2 and first
The raw material gas inlet of 3 middle and lower part of rectifying column is entered in first rectifying column 3；The raw material gas inlet of 3 middle and lower part of the first rectifying column
Going out unstripped gas temperature is：80℃；
Step 3：The unstripped gas entered in first rectifying column 3 described in step 2 is made to pass through the one or three with overhead condenser 5
Logical 13 and 3 top of first rectifying column fluid inlet in enter the low-boiling point material of first rectifying column 3 and carry out mass-and heat-transfer, mass transfer
The condensed rear liquid-phase outlet for passing through 3 bottom of first rectifying column of high boiling substance after heat transfer is entered in catcher 4, its low boiling
Material is entered in overhead condenser 5 by the gas phase import of gaseous phase outlet and overhead condenser 5 at the top of first rectifying column 3；Institute
The high boiling substance component stated in the catcher 4 of entrance is：Carbon dioxide 35%, alcohol 9.9%, water 55%, hydro carbons 0.1%, temperature
Spend and be：80 DEG C, pressure is 6Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser 5 described in step 3 is made by the first threeway 13, one
Enter in the fluid inlet on 3 top of liquid phase Jing first rectifying column of part low-boiling point material in first rectifying column 3 and the first rectification
Unstripped gas in tower 3 carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing
8th, the 3rd threeway 15, the first regulating valve 10 and 9 middle part inlet of Second distillation column enter the inside of Second distillation column 9；Second tunnel
Jing the second reboilers 8, the 3rd threeway 15 and the second regulating valve 11 enter the tube side of the second heat exchanger 6；It is described to enter the second rectification
The liquidus temperature of the low-boiling point material inside tower 9 is：5 DEG C, pressure is 6Mpa, and flow is 748Nm3/h；The rectifying column tower top
The liquid phase component of low-boiling point material in condenser 5：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are 5 DEG C, and pressure is
4.8Mpa；Liquidus temperature into the low-boiling point material of 6 tube side of the second heat exchanger is：- 30 DEG C, pressure is 2.0Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column 9 described in step 4 and pass through gas-liquid
The carbon dioxide that the fluid inlet on 9 top of liquid-phase outlet and Second distillation column of 7 bottom of separator is entered in Second distillation column 9 is rich
Liquid carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gaseous phase outlet row at the top of Second distillation column 9
Go out Second distillation column 9, its secondary high boiling substance is entered by the liquid-phase outlet of 9 bottom of Second distillation column, First Heat Exchanger 12
The liquid outlet of liquid mouth and First Heat Exchanger 12 is entered in carbon dioxide storage tank 16；The liquid-phase outlet of 9 bottom of the Second distillation column
Secondary high boiling substance component is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 10 DEG C, pressure is
3.0Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger 12 is：- 10～-20 DEG C, pressure is：
3.0Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger 12 is：- 15 DEG C, pressure is：3.0Mpa；Institute
State into the secondary high boiling substance in carbon dioxide storage tank 16 and be food-grade carbon-dioxide, its carbon dioxide content is
99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser 5 described in step 3 is made to pass through 5 gas of overhead condenser
Mutually outlet and the second threeway 14 is entered in the shell side of the second heat exchanger 6, makes the secondary of Second distillation column 9 is discharged described in step 5
The gas phase of low-boiling point material is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase and two of low-boiling point material
The gas phase of secondary low-boiling point material is entered in gas-liquid separator 7 in the gas phase after mixed heat transfer in the shell side of the second heat exchanger 6；It is described
The gaseous component of the low-boiling point material of 5 gaseous phase outlet of overhead condenser is carbon dioxide 65%, and temperature is：0 DEG C, pressure is：
4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column 9 is：Carbon dioxide 91%, hydrogen 1%, oxygen
2.1%, nitrogen 5.9%, temperature is：0 DEG C, pressure is 2.5Mpa；Gas in second heat exchanger, 6 shell side after mixed heat transfer
Temperature is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer is made to carry out gas-liquid separation, gas
The liquid phase on liquid-phase outlet and Second distillation column 9 top of the carbon dioxide rich solution after liquid separation by 7 bottom of gas-liquid separator is entered
Mouth is entered in Second distillation column 9, and the waste gas after gas-liquid separation is by the gaseous phase outlet at the top of gas-liquid separator 7, First Heat Exchanger
12 the first gas phase import 18 and the first gaseous phase outlet 19 of First Heat Exchanger 12 enter waste gas header 17；It is described go out gas-liquid separation
The carbon dioxide rich solution component of the liquid-phase outlet of 7 bottom of device is：Carbon dioxide 90%, temperature is：- 10 DEG C, pressure is 3.0MPa；
It is described go out gas-liquid separator 7 at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 52%, temperature are -10 DEG C, and pressure is
3.0MPa；
Step 8：The liquid phase described in step 4 into the low-boiling point material of 6 tube side of the second heat exchanger is made to pass sequentially through the
Second gaseous phase outlet 21 of two heat exchangers, 6 tube side, the second gas phase import 20 of First Heat Exchanger 12 and First Heat Exchanger 12 is entered
The two-stage compression air inlet of unstripped gas four-stage compressor 1；The two-stage compression air inlet of the entrance unstripped gas four-stage compressor 1
The liquidus temperature of low-boiling point material is：- 14 DEG C, pressure is 2.0Mpa.
Embodiment three
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank 22 and unstripped gas four-stage compressor 1 enters 2 import of the first reboiler,
The component of the unstripped gas is：Carbon dioxide 97%, water 0.4%, alcohol 2%, hydrocarbon 0.6%, temperature is：25 DEG C, pressure is：
0.15Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：105 DEG C, pressure is 5Mpa；
Step 2：Make to enter 2 imported materials gas of the first reboiler described in step one by the first reboiler 2 and first
The raw material gas inlet of 3 middle and lower part of rectifying column is entered in first rectifying column 3；The raw material gas inlet of 3 middle and lower part of the first rectifying column
Going out unstripped gas temperature is：55℃；
Step 3：The unstripped gas entered in first rectifying column 3 described in step 2 is made to pass through the one or three with overhead condenser 5
Logical 13 and 3 top of first rectifying column fluid inlet in enter the low-boiling point material of first rectifying column 3 and carry out mass-and heat-transfer, mass transfer
The condensed rear liquid-phase outlet for passing through 3 bottom of first rectifying column of high boiling substance after heat transfer is entered in catcher 4, its low boiling
Material is entered in overhead condenser 5 by the gas phase import of gaseous phase outlet and overhead condenser 5 at the top of first rectifying column 3；Institute
The high boiling substance component stated in the catcher 4 of entrance is：Carbon dioxide 32.5%, alcohol 8%, water 59%, hydro carbons 0.5%, temperature
Spend and be：65 DEG C, pressure is 5Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser 5 described in step 3 is made by the first threeway 13, one
Enter in the fluid inlet on 3 top of liquid phase Jing first rectifying column of part low-boiling point material in first rectifying column 3 and the first rectification
Unstripped gas in tower 3 carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing
8th, the 3rd threeway 15, the first regulating valve 10 and 9 middle part inlet of Second distillation column enter the inside of Second distillation column 9；Second tunnel
Jing the second reboilers 8, the 3rd threeway 15 and the second regulating valve 11 enter the tube side of the second heat exchanger 6；It is described to enter the second rectification
The liquidus temperature of the low-boiling point material inside tower 9 is：- 2.5 DEG C, pressure is 5Mpa, and flow is 748Nm3/h；The rectifying tower
The liquid phase component of low-boiling point material in the condenser 5 of top：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are -2.5 DEG C, pressure
Power is 4.8Mpa；Liquidus temperature into the low-boiling point material of 6 tube side of the second heat exchanger is：- 37.5 DEG C, pressure is 1.5Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column 9 described in step 4 and pass through gas-liquid
The carbon dioxide that the fluid inlet on 9 top of liquid-phase outlet and Second distillation column of 7 bottom of separator is entered in Second distillation column 9 is rich
Liquid carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gaseous phase outlet row at the top of Second distillation column 9
Go out Second distillation column 9, its secondary high boiling substance is entered by the liquid-phase outlet of 9 bottom of Second distillation column, First Heat Exchanger 12
The liquid outlet of liquid mouth and First Heat Exchanger 12 is entered in carbon dioxide storage tank 16；The liquid-phase outlet of 9 bottom of the Second distillation column
Secondary high boiling substance component is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 15 DEG C, pressure is
2.1Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger 12 is：- 10～-20 DEG C, pressure is：
2.2Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger 12 is：- 17.5 DEG C, pressure is：2.1Mpa；
Secondary high boiling substance in the entrance carbon dioxide storage tank 16 is food-grade carbon-dioxide, and its carbon dioxide content is
99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser 5 described in step 3 is made to pass through 5 gas of overhead condenser
Mutually outlet and the second threeway 14 is entered in the shell side of the second heat exchanger 6, makes the secondary of Second distillation column 9 is discharged described in step 5
The gas phase of low-boiling point material is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase and two of low-boiling point material
The gas phase of secondary low-boiling point material is entered in gas-liquid separator 7 in the gas phase after mixed heat transfer in the shell side of the second heat exchanger 6；It is described
The gaseous component of the low-boiling point material of 5 gaseous phase outlet of overhead condenser is carbon dioxide 57.5%, and temperature is：- 5 DEG C, pressure is：
4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column 9 is：Carbon dioxide 91%, hydrogen 1%, oxygen
2.1%, nitrogen 5.9%, temperature is：- 7.5 DEG C, pressure is 1.7Mpa；In second heat exchanger, 6 shell side after mixed heat transfer
Gas temperature is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer is made to carry out gas-liquid separation, gas
The liquid phase on liquid-phase outlet and Second distillation column 9 top of the carbon dioxide rich solution after liquid separation by 7 bottom of gas-liquid separator is entered
Mouth is entered in Second distillation column 9, and the waste gas after gas-liquid separation is by the gaseous phase outlet at the top of gas-liquid separator 7, First Heat Exchanger
12 the first gas phase import 18 and the first gaseous phase outlet 19 of First Heat Exchanger 12 enter waste gas header 17；It is described go out gas-liquid separation
The carbon dioxide rich solution component of the liquid-phase outlet of 7 bottom of device is：Carbon dioxide 85%, temperature is：- 21 DEG C, pressure is 2.3MPa；
It is described go out gas-liquid separator 7 at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 41%, temperature are -21 DEG C, and pressure is
2.3MPa；
Step 8：The liquid phase described in step 4 into the low-boiling point material of 6 tube side of the second heat exchanger is made to pass sequentially through the
Second gaseous phase outlet 21 of two heat exchangers, 6 tube side, the second gas phase import 20 of First Heat Exchanger 12 and First Heat Exchanger 12 is entered
The two-stage compression air inlet of unstripped gas four-stage compressor 1；The two-stage compression air inlet of the entrance unstripped gas four-stage compressor 1
The liquidus temperature of low-boiling point material is：- 14 DEG C, pressure is 1.5Mpa.
Example IV
A kind of method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification, comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank 22 and unstripped gas four-stage compressor 1 enters 2 import of the first reboiler,
The component of the unstripped gas is：Carbon dioxide 98.1%, water 1%, alcohol 0.4%, hydrocarbon 0.5%, flow is：770Nm3/ h, temperature
For：40 DEG C, pressure is：0.12Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor 1 is：100 DEG C, pressure is
4.8Mpa；
Step 2：Make to enter 2 imported materials gas of the first reboiler described in step one by the first reboiler 2 and first
The raw material gas inlet of 3 middle and lower part of rectifying column is entered in first rectifying column 3；The raw material gas inlet of 3 middle and lower part of the first rectifying column
Going out unstripped gas temperature is：65℃；
Step 3：The unstripped gas entered in first rectifying column 3 described in step 2 is made to pass through the one or three with overhead condenser 5
Logical 13 and 3 top of first rectifying column fluid inlet in enter the low-boiling point material of first rectifying column 3 and carry out mass-and heat-transfer, mass transfer
The condensed rear liquid-phase outlet for passing through 3 bottom of first rectifying column of high boiling substance after heat transfer is entered in catcher 4, its low boiling
Material is entered in overhead condenser 5 by the gas phase import of gaseous phase outlet and overhead condenser 5 at the top of first rectifying column 3；Institute
The high boiling substance component stated in the catcher 4 of entrance is：Carbon dioxide 31.8%, alcohol 10.3%, water 57.8%, hydro carbons
0.1%, temperature is：69.4 DEG C, pressure is 4.8Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser 5 described in step 3 is made by the first threeway 13, one
Enter in the fluid inlet on 3 top of liquid phase Jing first rectifying column of part low-boiling point material in first rectifying column 3 and the first rectification
Unstripped gas in tower 3 carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, the second reboiler of first via Jing
8th, the 3rd threeway 15, the first regulating valve 10 and 9 middle part inlet of Second distillation column enter the inside of Second distillation column 9；Second tunnel
Jing the second reboilers 8, the 3rd threeway 15 and the second regulating valve 11 enter the tube side of the second heat exchanger 6；It is described to enter the second rectification
The liquidus temperature of the low-boiling point material inside tower 9 is：- 10 DEG C, pressure is 4.8Mpa, and flow is 748Nm3/h；The rectifying column
The liquid phase component of low-boiling point material in overhead condenser 5：Carbon dioxide 99.3%, foreign gas 0.7%, temperature are -5 DEG C, pressure
Power is 4.8Mpa；Liquidus temperature into the low-boiling point material of 6 tube side of the second heat exchanger is：- 34.5 DEG C, pressure is 1.26Mpa；
Step 5：Make the liquid phase of the low-boiling point material entered inside Second distillation column 9 described in step 4 and pass through gas-liquid
The carbon dioxide that the fluid inlet on 9 top of liquid-phase outlet and Second distillation column of 7 bottom of separator is entered in Second distillation column 9 is rich
Liquid carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gaseous phase outlet row at the top of Second distillation column 9
Go out Second distillation column 9, its secondary high boiling substance is entered by the liquid-phase outlet of 9 bottom of Second distillation column, First Heat Exchanger 12
The liquid outlet of liquid mouth and First Heat Exchanger 12 is entered in carbon dioxide storage tank 16；The liquid-phase outlet of 9 bottom of the Second distillation column
Secondary high boiling substance component is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature is：- 12.1 DEG C, pressure is
2.5Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger 12 is：- 10～-20 DEG C, pressure is：
2.5Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger 12 is：- 15 DEG C, pressure is：2.5Mpa；Institute
State into the secondary high boiling substance in carbon dioxide storage tank 16 and be food-grade carbon-dioxide, its carbon dioxide content is
99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser 5 described in step 3 is made to pass through 5 gas of overhead condenser
Mutually outlet and the second threeway 14 is entered in the shell side of the second heat exchanger 6, makes the secondary of Second distillation column 9 is discharged described in step 5
The gas phase of low-boiling point material is entered in the shell side of the second heat exchanger 6 by the second threeway 14, makes the gas phase and two of low-boiling point material
The gas phase of secondary low-boiling point material is entered in gas-liquid separator 7 in the gas phase after mixed heat transfer in the shell side of the second heat exchanger 6；It is described
The gaseous component of the low-boiling point material of 5 gaseous phase outlet of overhead condenser is carbon dioxide 63.1%, and temperature is：- 5 DEG C, pressure is：
4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column 9 is：Carbon dioxide 91%, hydrogen 1%, oxygen
2.1%, nitrogen 5.9%, temperature is：- 15.2 DEG C, pressure is 2.5Mpa；In second heat exchanger, 6 shell side after mixed heat transfer
Gas temperature is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：The gas phase entered described in step 6 in gas-liquid separator 7 after mixed heat transfer is made to carry out gas-liquid separation, gas
The liquid phase on liquid-phase outlet and Second distillation column 9 top of the carbon dioxide rich solution after liquid separation by 7 bottom of gas-liquid separator is entered
Mouth is entered in Second distillation column 9, and the waste gas after gas-liquid separation is by the gaseous phase outlet at the top of gas-liquid separator 7, First Heat Exchanger
12 the first gas phase import 18 and the first gaseous phase outlet 19 of First Heat Exchanger 12 enter waste gas header 17；It is described go out gas-liquid separation
The carbon dioxide rich solution component of the liquid-phase outlet of 7 bottom of device is：Carbon dioxide 88.2%, temperature is：- 32 DEG C, pressure is
2.5MPa；It is described go out gas-liquid separator 7 at the top of the waste gas component of gaseous phase outlet be：Carbon dioxide 43.8%, temperature are -32
DEG C, pressure is 2.5MPa；
Step 8：The liquid phase described in step 4 into the low-boiling point material of 6 tube side of the second heat exchanger is made to pass sequentially through the
Second gaseous phase outlet 21 of two heat exchangers, 6 tube side, the second gas phase import 20 of First Heat Exchanger 12 and First Heat Exchanger 12 is entered
The two-stage compression air inlet of unstripped gas four-stage compressor 1；The two-stage compression air inlet of the entrance unstripped gas four-stage compressor 1
The liquidus temperature of low-boiling point material is：- 14 DEG C, pressure is 1.26Mpa.
Above-described embodiment is only intended to clearly illustrate example, and the not restriction to embodiment.For institute
For the general technical staff in category field, the change or change of other multi-forms can also be made on the basis of the above description
It is dynamic.There is no need to be exhaustive to all of embodiment, and thus it is amplified obvious change or change
Among moving still in the invention scope of the claims.
Claims (3)
1. the device of food-class liquid CO 2 is produced in a kind of utilization two-tower rectification purification, it is characterised in that：The device includes
Air inlet surge tank (22), air inlet surge tank (22) outlet are connected with the import of unstripped gas four-stage compressor (1) by pipeline, raw material
The outlet of gas four-stage compressor (1) is connected with the raw material gas inlet of first rectifying column (3) middle and lower part by the first reboiler (2),
The liquid-phase outlet of first rectifying column (3) bottom is connected with catcher (4), the gaseous phase outlet and tower top at the top of first rectifying column (3)
The gas phase import of condenser (5) is connected, and the liquid-phase outlet of overhead condenser (5) is by pipeline and first rectifying column (3) top
Fluid inlet is connected, on the pipeline between the liquid-phase outlet of overhead condenser (5) and the fluid inlet on first rectifying column (3) top
Be provided with the first threeway (13), the 3rd end of the first threeway (13) by pipeline successively with the second reboiler (8), the first regulating valve
(10) it is connected with inlet in the middle part of Second distillation column (9)；The liquid-phase outlet of Second distillation column (9) bottom is changed with first by pipeline
The inlet of hot device (12) is connected, and the liquid outlet of First Heat Exchanger (12) is connected with carbon dioxide storage tank (16)；The tower top is cold
Gaseous phase outlet at the top of condenser (5) passes through the shell side and gas-liquid separator (7) phase of the second threeway (14) and the second heat exchanger (6)
Even, the liquid-phase outlet of gas-liquid separator (7) bottom is connected with the fluid inlet on Second distillation column (9) top by pipeline, gas-liquid
Gaseous phase outlet at the top of separator (7) is connected with the first gas phase import (18) of First Heat Exchanger (12), First Heat Exchanger (12)
The first gaseous phase outlet (19) be connected with waste gas header (17)；Gaseous phase outlet at the top of the Second distillation column (9) passes through pipeline
It is connected with the 3rd end of the second threeway (14)；Pipeline between second reboiler (8) and the first regulating valve (10) is provided with
3rd threeway (15), the 3rd end of the 3rd threeway (15) pass through the tube side of the second regulating valve (11) and the second heat exchanger (6)
It is connected with the second gas phase import (20) of First Heat Exchanger (12), second gaseous phase outlet (21) of First Heat Exchanger (12) is by pipe
Road is connected with the two-stage compression air inlet of unstripped gas four-stage compressor (1).
2. the side of food-class liquid CO 2 device is produced in a kind of utilization two-tower rectification purification according to claim 1
Method, it is characterised in that：The method comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank (22) and unstripped gas four-stage compressor (1) enters into the first reboiler (2)
Mouthful, the component of the unstripped gas is：Carbon dioxide 95～99%, water 0.4～2%, alcohol 0.1～2%, hydrocarbon 0.1～1%, temperature
For：10～40 DEG C, pressure is：0.1～0.2Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor (1) is：90
～120 DEG C, pressure is 4～6Mpa；
Step 2：Make to enter the first reboiler (2) imported materials gas described in step one by the first reboiler (2) and first
The raw material gas inlet of rectifying column (3) middle and lower part is entered in first rectifying column (3)；The raw material of first rectifying column (3) middle and lower part
Gas import goes out unstripped gas temperature：30～80 DEG C；
Step 3：The unstripped gas and the overhead condenser (5) that enter in first rectifying column (3) described in step 2 are made by the one or three
The low-boiling point material that first rectifying column (3) is entered in the fluid inlet on logical (13) and first rectifying column (3) top carries out mass transfer biography
Heat, enters catcher (4) by the liquid-phase outlet of first rectifying column (3) bottom after the high boiling substance after mass-and heat-transfer is condensed
Interior, its low-boiling point material enters tower by the gas phase import of the gaseous phase outlet at the top of first rectifying column (3) and overhead condenser (5)
In top condenser (5)；High boiling substance component in the catcher (4) of the entrance is：Carbon dioxide 30～35%, alcohol 5～
11%, water 40～60%, hydro carbons 0.1～1%, temperature is：50～80 DEG C, pressure is 4～6Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser described in step 3 (5) is made by the first threeway (13), one
Enter in the fluid inlet on liquid phase Jing first rectifying column (3) top of part low-boiling point material in first rectifying column (3) with first
Unstripped gas in rectifying column (3) carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, first via Jing second
In the middle part of reboiler (8), the 3rd threeway (15), the first regulating valve (10) and Second distillation column (9), inlet enters Second distillation column
(9) inside；Second the second reboiler of tunnel (8), the 3rd threeway (15) and the second regulating valve (11) are into the second heat exchanger (6)
Tube side；The liquidus temperature of the internal low-boiling point material of the entrance Second distillation column (9) is：5～-10 DEG C, pressure be 4～
6Mpa, flow are 748Nm3/h；The liquid phase component of low-boiling point material in the rectifying column tower top condenser (5)：Carbon dioxide
99.3%, foreign gas 0.7%, temperature are 5～-10 DEG C, and pressure is 4.8Mpa；Into the low boiling of the second heat exchanger (6) tube side
Point material liquidus temperature be：- 30～-45 DEG C, pressure is 1.0～2.0Mpa；
Step 5：Make the liquid phase of the internal low-boiling point material of Second distillation column (9) to be entered described in step 4 and is divided by gas-liquid
From the titanium dioxide that the liquid-phase outlet of device (7) bottom and the fluid inlet on Second distillation column (9) top are entered in Second distillation column (9)
Carbon rich solution carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gas phase at the top of Second distillation column (9)
Second distillation column (9) is discharged in outlet, and its secondary high boiling substance is changed by the liquid-phase outlet of Second distillation column (9) bottom, first
The liquid outlet of the inlet and First Heat Exchanger (12) of hot device (12) is entered in carbon dioxide storage tank (16)；The Second distillation column
(9) the secondary high boiling substance component of the liquid-phase outlet of bottom is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature
For：- 10～-20 DEG C, pressure is 1.5～3.0Mpa；The secondary high boiling substance of the inlet of the First Heat Exchanger (12)
Temperature is：- 10～-20 DEG C, pressure is：1.5～3.0Mpa；The secondary high boiling substance of liquid outlet of the First Heat Exchanger (12)
Temperature be：- 15 DEG C～-20 DEG C, pressure is：1.5～3.0Mpa；Secondary height boiling in the entrance carbon dioxide storage tank (16)
Point material is food-grade carbon-dioxide, and its carbon dioxide content is 99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser described in step 3 (5) is made to pass through overhead condenser (5) gas
Mutually outlet and the second threeway (14) in the shell side of the second heat exchanger (6) makes Second distillation column (9) is discharged described in step 5
Secondary low-boiling point material gas phase by the second threeway (14) in the shell side of the second heat exchanger (6), make low-boiling point material
Gas phase and secondary low-boiling point material gas phase of the gas phase after mixed heat transfer in the shell side of the second heat exchanger (6) into gas-liquid point
In device (7)；The gaseous component of the low-boiling point material of overhead condenser (5) gaseous phase outlet is carbon dioxide 50～65%,
Temperature is：0～-10 DEG C, pressure is：4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column (9) is：
Carbon dioxide 91%, hydrogen 1%, oxygen 2.1%, nitrogen 5.9%, temperature is：0～-15 DEG C, pressure is 1.0～2.5Mpa；Institute
Stating the gas temperature in the second heat exchanger (6) shell side after mixed heat transfer is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：Gas phase after making the interior mixed heat transfer of gas-liquid separator (7) is entered described in step 6 carries out gas-liquid separation, gas-liquid
The liquid phase of liquid-phase outlet and Second distillation column (9) top of the carbon dioxide rich solution after separation by gas-liquid separator (7) bottom
Import is entered in Second distillation column (9), the waste gas after gas-liquid separation by the gaseous phase outlet at the top of gas-liquid separator (7), first
First gas phase import (18) of heat exchanger (12) and first gaseous phase outlet (19) of First Heat Exchanger (12) enter waste gas header
(17)；It is described go out gas-liquid separator (7) bottom the carbon dioxide rich solution component of liquid-phase outlet be：Carbon dioxide 80～90%,
Temperature is：- 10～-32 DEG C, pressure is 1.5～3.0MPa；It is described go out gas-liquid separator (7) at the top of gaseous phase outlet waste gas group
It is divided into：Carbon dioxide 30～52%, temperature are -10～-32 DEG C, and pressure is 1.5～3.0MPa；
Step 8：The liquid phase of the low-boiling point material described in step 4 into the second heat exchanger (6) tube side is made to pass sequentially through second
Heat exchanger (6) tube side, the second gas phase import (20) of First Heat Exchanger (12) and the second gaseous phase outlet of First Heat Exchanger (12)
(21) into the two-stage compression air inlet of unstripped gas four-stage compressor (1)；Two grades of the entrance unstripped gas four-stage compressor (1)
The liquidus temperature of the low-boiling point material of compressed air inlet is：- 14 DEG C, pressure is 1.0～2.0Mpa.
3. the method that food-class liquid CO 2 device is produced in utilization two-tower rectification purification according to claim 2, its
It is characterised by：The method comprises the steps：
Step one：Unstripped gas passes through air inlet surge tank (22) and unstripped gas four-stage compressor (1) enters into the first reboiler (2)
Mouthful, the component of the unstripped gas is：Carbon dioxide 98.1%, water 1%, alcohol 0.4%, hydrocarbon 0.5%, flow is：770Nm3/ h, temperature
Spend and be：40 DEG C, pressure is：0.12Mpa；The unstripped gas by the temperature after unstripped gas four-stage compressor (1) is：100 DEG C, pressure
Power is 4.8Mpa；
Step 2：Make to enter the first reboiler (2) imported materials gas described in step one by the first reboiler (2) and first
The raw material gas inlet of rectifying column (3) middle and lower part is entered in first rectifying column (3)；The raw material of first rectifying column (3) middle and lower part
Gas import goes out unstripped gas temperature：65℃；
Step 3：The unstripped gas and the overhead condenser (5) that enter in first rectifying column (3) described in step 2 are made by the one or three
The low-boiling point material that first rectifying column (3) is entered in the fluid inlet on logical (13) and first rectifying column (3) top carries out mass transfer biography
Heat, enters catcher (4) by the liquid-phase outlet of first rectifying column (3) bottom after the high boiling substance after mass-and heat-transfer is condensed
Interior, its low-boiling point material enters tower by the gas phase import of the gaseous phase outlet at the top of first rectifying column (3) and overhead condenser (5)
In top condenser (5)；High boiling substance component in the catcher (4) of the entrance is：Carbon dioxide 31.8%, alcohol
10.3%, water 57.8%, hydro carbons 0.1%, temperature is：69.4 DEG C, pressure is 4.8Mpa；
Step 4：The liquid phase of low-boiling point material in overhead condenser described in step 3 (5) is made by the first threeway (13), one
Enter in the fluid inlet on liquid phase Jing first rectifying column (3) top of part low-boiling point material in first rectifying column (3) with first
Unstripped gas in rectifying column (3) carries out mass-and heat-transfer, and the liquid phase of another part low-boiling point material is divided into two-way, first via Jing second
In the middle part of reboiler (8), the 3rd threeway (15), the first regulating valve (10) and Second distillation column (9), inlet enters Second distillation column
(9) inside；Second the second reboiler of tunnel (8), the 3rd threeway (15) and the second regulating valve (11) are into the second heat exchanger (6)
Tube side；The liquidus temperature of the internal low-boiling point material of the entrance Second distillation column (9) is：- 10 DEG C, pressure is 4.8Mpa,
Flow is 748Nm3/h；The liquid phase component of low-boiling point material in the rectifying column tower top condenser (5)：Carbon dioxide 99.3%,
Foreign gas 0.7%, temperature are -5 DEG C, and pressure is 4.8Mpa；Into the liquid phase of the low-boiling point material of the second heat exchanger (6) tube side
Temperature is：- 34.5 DEG C, pressure is 1.26Mpa；
Step 5：Make the liquid phase of the internal low-boiling point material of Second distillation column (9) to be entered described in step 4 and is divided by gas-liquid
From the titanium dioxide that the liquid-phase outlet of device (7) bottom and the fluid inlet on Second distillation column (9) top are entered in Second distillation column (9)
Carbon rich solution carries out mass-and heat-transfer, and after mass-and heat-transfer, the gas phase of secondary low-boiling point material is by the gas phase at the top of Second distillation column (9)
Second distillation column (9) is discharged in outlet, and its secondary high boiling substance is changed by the liquid-phase outlet of Second distillation column (9) bottom, first
The liquid outlet of the inlet and First Heat Exchanger (12) of hot device (12) is entered in carbon dioxide storage tank (16)；The Second distillation column
(9) the secondary high boiling substance component of the liquid-phase outlet of bottom is：Carbon dioxide 99.99%, flow is：666Nm3/ h, temperature
For：- 12.1 DEG C, pressure is 2.5Mpa；The temperature of the secondary high boiling substance of the inlet of the First Heat Exchanger (12) is：-
10～-20 DEG C, pressure is：2.5Mpa；The temperature of the secondary high boiling substance of liquid outlet of the First Heat Exchanger (12) is：-15
DEG C, pressure is：2.5Mpa；Secondary high boiling substance in the entrance carbon dioxide storage tank (16) is food stage titanium dioxide
Carbon, its carbon dioxide content are 99.99%；
Step 6：The gas phase of the low-boiling point material in overhead condenser described in step 3 (5) is made to pass through overhead condenser (5) gas
Mutually outlet and the second threeway (14) in the shell side of the second heat exchanger (6) makes Second distillation column (9) is discharged described in step 5
Secondary low-boiling point material gas phase by the second threeway (14) in the shell side of the second heat exchanger (6), make low-boiling point material
Gas phase and secondary low-boiling point material gas phase of the gas phase after mixed heat transfer in the shell side of the second heat exchanger (6) into gas-liquid point
In device (7)；The gaseous component of the low-boiling point material of overhead condenser (5) gaseous phase outlet is carbon dioxide 63.1%, warm
Spend and be：- 5 DEG C, pressure is：4.8Mpa；The gaseous component of the secondary low-boiling point material of the Second distillation column (9) is：Titanium dioxide
Carbon 91%, hydrogen 1%, oxygen 2.1%, nitrogen 5.9%, temperature is：- 15.2 DEG C, pressure is 2.5Mpa；Second heat exchanger
(6) gas temperature in shell side after mixed heat transfer is：- 30 DEG C, pressure is：1.26Mpa；
Step 7：Gas phase after making the interior mixed heat transfer of gas-liquid separator (7) is entered described in step 6 carries out gas-liquid separation, gas-liquid
The liquid phase of liquid-phase outlet and Second distillation column (9) top of the carbon dioxide rich solution after separation by gas-liquid separator (7) bottom
Import is entered in Second distillation column (9), the waste gas after gas-liquid separation by the gaseous phase outlet at the top of gas-liquid separator (7), first
First gas phase import (18) of heat exchanger (12) and first gaseous phase outlet (19) of First Heat Exchanger (12) enter waste gas header
(17)；It is described go out gas-liquid separator (7) bottom the carbon dioxide rich solution component of liquid-phase outlet be：Carbon dioxide 88.2%, temperature
Spend and be：- 32 DEG C, pressure is 2.5MPa；It is described go out gas-liquid separator (7) at the top of the waste gas component of gaseous phase outlet be：Titanium dioxide
Carbon 43.8%, temperature are -32 DEG C, and pressure is 2.5MPa；
Step 8：The liquid phase of the low-boiling point material described in step 4 into the second heat exchanger (6) tube side is made to pass sequentially through second
Heat exchanger (6) tube side, the second gas phase import (20) of First Heat Exchanger (12) and the second gaseous phase outlet of First Heat Exchanger (12)
(21) into the two-stage compression air inlet of unstripped gas four-stage compressor (1)；Two grades of the entrance unstripped gas four-stage compressor (1)
The liquidus temperature of the low-boiling point material of compressed air inlet is：- 14 DEG C, pressure is 1.26Mpa.
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| CN107673351B (en) * | 2017-11-20 | 2019-06-18 | 惠州凯美特气体有限公司 | A kind of production method of high-pureness carbon dioxide |
| CN110057164B (en) * | 2019-03-20 | 2023-05-19 | 河南心连心深冷能源股份有限公司 | Production of electronic grade CO with water content less than or equal to 30ppb 2 Apparatus and method of production of (a) |
| CN110243137B (en) * | 2019-05-22 | 2021-07-16 | 陈剑军 | Device and method for producing food-grade CO2 by adopting NH3/CO2 cascade refrigeration |
| CN110440526A (en) * | 2019-07-27 | 2019-11-12 | 江西江氨科技有限公司 | Food-grade carbon-dioxide preparation system |
| WO2021016779A1 (en) * | 2019-07-27 | 2021-02-04 | 江西江氨科技有限公司 | Food-grade co2 preparation system |
| CN111256432B (en) * | 2020-03-12 | 2024-03-08 | 金昌隆博气体有限责任公司 | Device and method for treating waste liquid from carbon dioxide rectification separation |
| CN111977654B (en) * | 2020-10-21 | 2024-05-24 | 重庆瑞信气体有限公司 | CO is retrieved in low temperature methanol washing workshop section2Is a device and process thereof |
| CN114669167A (en) * | 2022-02-16 | 2022-06-28 | 苏州市兴鲁空分设备科技发展有限公司 | Pressure swing adsorption and desorption gas recycling device |
| CN115072722B (en) * | 2022-07-05 | 2023-04-25 | 重庆朗福环保科技有限公司 | Edible carbon dioxide liquefaction preparation method and device thereof |
| CN116531788A (en) * | 2023-06-20 | 2023-08-04 | 泰兴市凌飞化学科技有限公司 | Nonylphenol polyoxyethylene ether rectification system and rectification method |
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| US8080090B2 (en) * | 2007-02-16 | 2011-12-20 | Air Liquide Process & Construction, Inc. | Process for feed gas cooling in reboiler during CO2 separation |
| GB2493400A (en) * | 2011-08-05 | 2013-02-06 | Bp Alternative Energy Internat Ltd | Separation of carbon dioxide and hydrogen |
| CN102765719B (en) * | 2012-07-25 | 2014-09-24 | 河南心连心深冷能源股份有限公司 | Technological method for co-producing industrial-grade carbon dioxide and food-grade carbon dioxide through heat pump rectification |
| CN102980374B (en) * | 2012-12-18 | 2016-06-22 | 杭州快凯高效节能新技术有限公司 | The preparation method of high purity liquid carbon dioxide and device |
| CN103277980B (en) * | 2013-06-13 | 2015-01-14 | 东南大学 | Carbon dioxide capture device utilizing both part oxygen-enriched combustion and nitrogen-and-oxygen separation |
| CN203938650U (en) * | 2014-05-19 | 2014-11-12 | 浙江工业大学 | A kind of biological aviation kerosene continuous rectification system based on shallow liquid layer vaporizer |
| CN204513904U (en) * | 2015-02-02 | 2015-07-29 | 河南心连心深冷能源股份有限公司 | Utilize two-tower rectification to purify and produce the device of food-class liquid CO 2 |
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