CN106147883B - A kind of method that solution circular regeneration improves recovery rate of CO 2 and purity - Google Patents
A kind of method that solution circular regeneration improves recovery rate of CO 2 and purity Download PDFInfo
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- CN106147883B CN106147883B CN201610613655.5A CN201610613655A CN106147883B CN 106147883 B CN106147883 B CN 106147883B CN 201610613655 A CN201610613655 A CN 201610613655A CN 106147883 B CN106147883 B CN 106147883B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/005—Carbon dioxide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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Abstract
The present invention relates to a kind of methods that solution circular regeneration improves recovery rate of CO 2 and purity, and during low-temp methanol is washed, poor methanol first passes around CO2Absorption tower absorbs CO2, it is rich in CO2Methanol solution through the invention after the regeneration measure of patent, on the one hand absorbed the CO of dissolving2It desorbs, obtains the high CO of purity2Product gas (CO299.9%) molar fraction >=99% reaches as high as, on the other hand obtain and contain CO2Measure lower half poor methanol solution (CO2Molar fraction≤8%), half barren solution after desorption is delivered to through pump in the middle part of carbon dioxide absorption tower, is recycled, high-purity CO2Product gas is then compressed to other workshop sections according to the requirement of technique.
Description
Technical field
The invention belongs to gas purification process technical fields, and in particular to a kind of solution circular regeneration raising carbon dioxide time
The method of yield and purity.
Background technology
In Chemical Manufacture, low-temp methanol, which is washed, is widely used in desulfurization and decarburization process, absorbs rough coal by low-temp methanol
Sour gas in gas, such as：CO2、H2S, the components such as COS, to achieve the purpose that purify raw gas.Absorbing has the first of sour gas component
Alcoholic solution can realize Mathanol regenerating by operational means such as vacuum flashing, nitrogen stripping, heating regeneration.In the process, H2S、
The sulfur-rich tail gas such as COS can realize the recycling of element sulphur through sulfur recovery unit, and CO2Gas then passes through vacuum flashing
Journey is enriched with, but is not easy to obtain the CO that purity is higher than 95%2Product gas.
Invention content
Present invention aim to address existing CO2Gas is not easy to obtain the high CO of purity by the enrichment of vacuum flashing process2Production
The technical issues of product gas, provides a kind of method that solution circular regeneration improves recovery rate of CO 2 and purity.
In order to solve the above technical problems, the technical solution adopted by the present invention is：
A kind of method that solution circular regeneration improves recovery rate of CO 2 and purity, includes the following steps：
(1)CO2It absorbs
The raw gas that pressure is 3.0~6.0Mpa is removed into H by hydrogen sulfide absorption tower first2Sulphur member in S and COS
Element then enters CO2Absorption tower, methanol lean solution is from CO2Absorbing tower top spray enters, and from CO2The sweet gas that absorbing tower bottom enters
Counter current contacting, in CO2Carbon dioxide eliminating is carried out in absorption tower, from CO2Solution is drawn in the middle part of absorption tower to cool down through two ammonia coolers
After return to CO2Improving CO in absorption tower2Solubility, CO2Absorption tower epimere introduces after flash column vacuum flashing half poor
Methanol solution is improving CO2Uptake, purified gas is from CO2Absorbing tower is lifted off out, into downstream process, CO2It absorbs
A rich carbon methanol solution part for tower bottom of tower outflow is sent to hydrogen sulfide absorption tower as desulfurization washing lotion, and another part is sent to flash column
To regenerated methanol, while recycling CO2As product gas；
In CO2When absorption tower carries out carbon dioxide eliminating, since absorption process can discharge heat of solution, methanol solution temperature meeting
Rise therewith, leads to the reduction of Solubilities of Carbon Dioxide, it is therefore desirable in CO2Absorbent solution warp is drawn at the intermediate tray of absorption tower
CO is returned after two ammonia cooler ammonia coolings2To improve CO in absorbing tower2Solubility, in CO2The epimere on absorption tower, which then introduces, to be subtracted
Half poor methanol solution after pressure flash distillation, to improve CO2Uptake, purified gas is from CO2Absorbing tower is lifted off out, and is entered
Downstream process, absorption have CO2Rich carbon methanol solution then a part is sent to hydrogen sulfide absorption tower as desulfurization washing lotion, another part
It then send to flash evaporation unit with regenerated methanol, while recycling CO2As product gas.
This step prevailing operating conditions：
CO2Absorption tower unstripped gas temperature：- 12~-30 DEG C
CO2Absorption tower operating pressure：30~60bar
Carbon dioxide content is less than 10ppm in product gas after decarburization.
(2) I sections of flash distillations and absorption
From CO2The rich carbon methanol solution on absorption tower is sent after decompression to I section of flash vessel positioned at flash distillation tower bottom, rich
Carbon methanol solution is flashed from the middle part of I section of flash vessel into I section of flash vessel, H2、N2、CO、Ar、CH4Inertia group is from solution
It flashes off, due to CO2Solubility is more than above-mentioned inert component, therefore CO2It can stay in rich carbon methanol solution, on I section of flash vessel
One of section introducing washs gas phase from half poor methanol after the flash distillation of IV section of flash vessel of flash column, to ensure CO2Recycling
Rate, the steaming liquid come out from I section of flash vessel bottom end are mutually sent under the action of itself pressure difference to II section of flash vessel of flash column, from I section
The flashed vapour that flash vessel top comes out goes to compress to be back in unstripped gas to recycle；
I section of flash distillation and absorption operation temperature：- 26~-31 DEG C；
I section of flash distillation and absorption operation pressure：9~15bar；
(3) II sections of flash distillations and absorption
Contain CO by I section of flash vessel2Methanol solution enters II section of flash vessel being located at the top of flash column, part CO2It is dodged
It is steamed out, and battery limit (BL), CO is sent out from flash column top export after the half poor methanol solution washing from IV section of flash vessel2Production
Product gas purity reaches 95% or more, contains CO after flash distillation2Methanol solution be then sent to III section of flash vessel of flash column and continue to dodge
It steams；
II section of flash distillation and absorption operation temperature：- 48~-53 DEG C；
II section of flash distillation and absorption operation pressure：1.4~3.0bar；
(4) III sections of flash distillations
Contain CO by what II section of flash vessel flashed2Methanol solution enters in III section of flash vessel being located at below II section of flash vessel
It is flashed, the CO flashed off2Product exports out from III section of flash vessel, CO2Purity of product gas reaches 99%, due to dioxy
Heat can be absorbed by changing the flash process of carbon, therefore operation temperature can further decrease, and contain CO after flash distillation2Methanol solution then by
It send to IV section of flash vessel and continues to flash；
III section of flash distillation and absorption operation temperature：- 60~-65 DEG C；
III section of flash distillation and absorption operation pressure：0.5~0.9bar；
(5) IV sections of flash distillations
Contain CO by III section of flash vessel2Methanol solution, which enters in IV section of flash vessel being located at below III section of flash vessel, to carry out
Flash distillation, the CO flashed off at this time2Product exports out from IV section of flash vessel, CO2Purity of product gas reaches 99.6%, after flash distillation
Half poor methanol be divided into four parts, first part is pumped up to CO2Absorption tower epimere is as absorption CO2It recycles, second part
It is pumped up to I section of flash vessel and recycles, Part III is pumped up to II section of flash vessel and recycles, and remaining part is sent to downstream
Process is as washing lotion；
This step prevailing operating conditions：
IV section of flashing operation temperature：- 70~-75 DEG C；
IV section of flashing operation pressure：0.25~0.4bar.
The present invention is had the following advantages compared with the background art using above technical scheme：
1) CO of high-purity has been recycled2, purity >=95mol%；
2) oil product in process gas has been recycled, as addition product, has improved industrial output value；
3) recycling fuel gas can recycle；
4) solvent methanol can recycle.
Description of the drawings
Attached drawing is the flow chart of the present invention
Specific implementation mode
Embodiment 1
The method that a kind of solution circular regeneration in the present embodiment improves recovery rate of CO 2 and purity, including following step
Suddenly：
(1)CO2It absorbs
The raw gas that pressure is 3.0Mpa is removed into H by hydrogen sulfide absorption tower first2Element sulphur in S and COS, comes from
The desulfurization rough coal throughput of hydrogen sulfide absorption tower is 280000Nm3/ h, temperature：- 30 DEG C, pressure：30bar, the specific gas of sweet gas
Body group becomes：
| Composition | H2 | N2 | CO | CH4 | CO2 | ∑ |
| V% | 43.6 | 0.72 | 17.7 | 9.9 | 28.08 | 100.0 |
Then enter CO2Absorption tower 1, methanol lean solution is from CO2Absorption tower 1 tower top sprays into, and from CO21 bottom of tower of absorption tower enters
Sweet gas counter current contacting, in CO2Carbon dioxide eliminating is carried out in absorption tower 1, from CO2Solution is drawn through two in 1 middle part of absorption tower
Ammonia cooler 2,3 returns to CO after cooling down2Improving CO in absorption tower 12Solubility, CO21 epimere of absorption tower is introduced through flash column
Half poor methanol liquid after vacuum flashing is improving CO2Uptake, carbon content reaches 10ppm in purified gas, purifies
Gas afterwards is from CO21 tower top of absorption tower leaves, into downstream process, CO2The rich carbon methanol solution one of 1 bottom of tower of absorption tower outflow
To hydrogen sulfide absorption tower as desulfurization washing lotion, another part is sent to flash column to regenerated methanol, while recycling CO for dispensing2As
Product gas；
In CO2When absorption tower 1 carries out carbon dioxide eliminating, since absorption process can discharge heat of solution, methanol solution temperature
It can rise therewith, lead to the reduction of Solubilities of Carbon Dioxide, it is therefore desirable in CO2It is molten that absorption is drawn at 1 intermediate tray of absorption tower
Liquid returns to CO after two ammonia coolers 2, the cooling of 3 ammonia2To improve CO in 1 tower of absorption tower2Solubility, in CO2Absorption tower 1 it is upper
Section then introduces half poor methanol solution after vacuum flashing, to improve CO2Uptake, purified gas is from CO21 tower of absorption tower
It is lifted off out, into downstream process, absorption has CO2Rich carbon methanol solution then a part is sent to hydrogen sulfide absorption tower and is washed as desulfurization
Liquid, another part is then sent to flash evaporation unit with regenerated methanol, while recycling CO2As product gas.
This step prevailing operating conditions：
CO2Absorption tower intake air temperature：-30℃
CO2Absorption tower operating pressure：30bar
(2) I sections of flash distillations and absorption
From CO2The rich carbon methanol solution on absorption tower 1 is sent after decompression to I section of flash vessel 4 positioned at flash distillation tower bottom,
Rich carbon methanol solution is flashed from the middle part of I section of flash vessel 4 into I section of flash vessel 4, H2、N2、CO、Ar、CH4Inertia group self-dissolving
It is flashed off in liquid, due to CO2Solubility is more than above-mentioned inert component, therefore CO2It can stay in rich carbon methanol solution, I section of flash distillation
One of 4 epimere of device introducing washs vapor phase from half poor methanol after the flash distillation of IV section of flash vessel 7 of flash column, to ensure
CO2The rate of recovery, the steaming liquid come out from I section of 4 bottom end of flash vessel mutually sent under the action of itself pressure difference to II section of sudden strain of a muscle of flash column
Steaming device 5, the flashed vapour come out from I section of 4 top of flash vessel go to compress to be back in unstripped gas to recycle, I section of flash distillation gas phase stream
Amount is 3877Nm3/h；
I section of flash distillation and absorption operation temperature：-31℃；
I section of flash distillation and absorption operation pressure：9bar；
(3) II sections of flash distillations and absorption
Contain CO by I section of flash vessel 42Methanol solution enters II section of flash vessel 5 being located at the top of flash column, part CO2Quilt
It flashes off, and battery limit (BL) is sent out from flash column top export after the half poor methanol solution washing from IV section of flash vessel 7, it should
The CO that section flashes off2Flow is 20000Nm3/ h, purity are 95.2%mol CO2Purity of product gas reaches 95% or more, flash distillation
Afterwards contain CO2Methanol solution be then sent to III section of flash vessel 6 of flash column and continue to flash,；
II section of flash distillation and absorption operation temperature：-53℃；
II section of flash distillation and absorption operation pressure：1.4bar；
(4) III sections of flash distillations
Contain CO by what II section of flash vessel 5 flashed2Methanol solution enters III section of flash vessel for being located at II section of 5 lower section of flash vessel
It is flashed in 6, the CO flashed off2Product comes out from III section of flash vessel 6, obtains CO2 product throughputs and is
21000Nm3/ h, purity 99.4%mol, since the flash process of carbon dioxide can absorb heat, operation temperature can be into
One step reduces, and contains CO after flash distillation2Methanol solution be then sent to IV section of flash vessel 7 and continue to flash；
III section of flash distillation and absorption operation temperature：-65℃；
III section of flash distillation and absorption operation pressure：0.5bar；
(5) IV sections of flash distillations
Contain CO by III section of flash vessel 62Methanol solution enters in IV section of flash vessel 7 for being located at III section of 6 lower section of flash vessel
It is flashed, the CO flashed off at this time2Product comes out from IV section of flash vessel 7, obtains CO2Product throughput is
9000Nm3/ h, purity 99.7%mol, half poor methanol after flash distillation are divided into four parts, and first part send through pump 8 to CO2It absorbs
1 epimere of tower is as absorption CO2It recycles, second part send to I section of flash vessel 4 through pump 10 and recycles, and Part III is through pump 9
It send to II section of flash vessel 5 and recycles, Part IV is sent to downstream process as washing lotion；
This step prevailing operating conditions：
IV section of flashing operation temperature：-75℃；
IV section of flashing operation pressure：0.25bar.
Embodiment 2
The method that a kind of solution circular regeneration in the present embodiment improves recovery rate of CO 2 and purity, including following step
Suddenly：
(1)CO2It absorbs
Raw gas is removed into H by hydrogen sulfide absorption tower first2Element sulphur in S and COS, from hydrogen sulfide absorption tower
Desulfurization rough coal throughput is 250000Nm3/ h, temperature：- 25 DEG C, pressure：45bar, the specific gas group of sweet gas become：
| Composition | H2 | N2 | CO | CH4 | CO2 | ∑ |
| V% | 40.6 | 0.79 | 20.0 | 8.98 | 29.63 | 100.0 |
Then enter CO2Absorption tower 1, methanol lean solution is from CO2Absorption tower 1 tower top sprays into, and from CO21 bottom of tower of absorption tower enters
Sweet gas counter current contacting, in CO2Carbon dioxide eliminating is carried out in absorption tower 1, from CO2Solution is drawn through two in 1 middle part of absorption tower
Ammonia cooler 2,3 returns to CO after cooling down2Improving CO in absorption tower 12Solubility, CO21 epimere of absorption tower is introduced through flash column
Half poor methanol liquid after vacuum flashing is improving CO2Uptake, carbon content reaches 10ppm in purified gas, purifies
Gas afterwards is from CO21 tower top of absorption tower leaves, into downstream process, CO2The rich carbon methanol solution one of 1 bottom of tower of absorption tower outflow
To hydrogen sulfide absorption tower as desulfurization washing lotion, another part is sent to flash column to regenerated methanol, while recycling CO for dispensing2As
Product gas；
In CO2When absorption tower 1 carries out carbon dioxide eliminating, since absorption process can discharge heat of solution, methanol solution temperature
It can rise therewith, lead to the reduction of Solubilities of Carbon Dioxide, it is therefore desirable in CO2It is molten that absorption is drawn at 1 intermediate tray of absorption tower
Liquid returns to CO after two ammonia coolers 2, the cooling of 3 ammonia2To improve CO in 1 tower of absorption tower2Solubility, in CO2Absorption tower 1 it is upper
Section then introduces half poor methanol solution after vacuum flashing, to improve CO2Uptake, purified gas is from CO21 tower of absorption tower
It is lifted off out, into downstream process, absorption has CO2Rich carbon methanol solution then a part is sent to hydrogen sulfide absorption tower and is washed as desulfurization
Liquid, another part is then sent to flash evaporation unit with regenerated methanol, while recycling CO2As product gas.
This step prevailing operating conditions：
CO2Absorption tower intake air temperature：-25℃；
CO2Absorption tower operating pressure：45bar；
(2) I sections of flash distillations and absorption
From CO2The rich carbon methanol solution on absorption tower 1 is sent after decompression to I section of flash vessel 4 positioned at flash distillation tower bottom,
Rich carbon methanol solution is flashed from the middle part of I section of flash vessel 4 into I section of flash vessel 4, H2、N2、CO、Ar、CH4Inertia group self-dissolving
It is flashed off in liquid, due to CO2Solubility is more than above-mentioned inert component, therefore CO2It can stay in rich carbon methanol solution, I section of flash distillation
One of 4 epimere of device introducing washs vapor phase from half poor methanol after the flash distillation of IV section of flash vessel 7 of flash column, to ensure
CO2The rate of recovery, the steaming liquid come out from I section of 4 bottom end of flash vessel mutually sent under the action of itself pressure difference to II section of sudden strain of a muscle of flash column
Steaming device 5, the flashed vapour come out from I section of 4 top of flash vessel go to compress to be back in unstripped gas to recycle, I section of flash distillation gas phase stream
Amount is 3534Nm3/h；
I section of flash distillation and absorption operation temperature：-28℃；
I section of flash distillation and absorption operation pressure：13bar；
(3) II sections of flash distillations and absorption
Contain CO by I section of flash vessel 42Methanol solution enters II section of flash vessel 5 being located at the top of flash column, part CO2Quilt
It flashes off, and battery limit (BL) is sent out from flash column top export after the half poor methanol solution washing from IV section of flash vessel 7, it should
The CO that section flashes off2Flow is 18000Nm3/ h, purity are 95.8%mol CO2Purity of product gas reaches 95% or more, flash distillation
Afterwards contain CO2Methanol solution be then sent to III section of flash vessel 6 of flash column and continue to flash；
II section of flash distillation and absorption operation temperature：-50℃；
II section of flash distillation and absorption operation pressure：2.0bar；
(4) III sections of flash distillations
Contain CO by what II section of flash vessel 5 flashed2Methanol solution enters III section of flash vessel for being located at II section of 5 lower section of flash vessel
It is flashed in 6, the CO flashed off2Product comes out from III section of flash vessel 6, obtains CO2Product throughput is
19000Nm3/ h, purity 99.3%mol, since the flash process of carbon dioxide can absorb heat, operation temperature can be into
One step reduces, and contains CO after flash distillation2Methanol solution be then sent to IV section of flash vessel 7 and continue to flash；
III section of flash distillation and absorption operation temperature：-62℃；
III section of flash distillation and absorption operation pressure：0.7bar；
(5) IV sections of flash distillations
Contain CO by III section of flash vessel 62Methanol solution enters in IV section of flash vessel 7 for being located at III section of 6 lower section of flash vessel
It is flashed, the CO flashed off at this time2Product comes out from IV section of flash vessel 7, obtains CO2Product throughput is
8000Nm3/ h, purity 99.65%mol, half poor methanol after flash distillation are divided into four parts, and first part send through pump 8 to CO2It absorbs
1 epimere of tower is as absorption CO2It recycles, second part send to I section of flash vessel 4 through pump 10 and recycles, and Part III is through pump 9
It send to II section of flash vessel 5 and recycles, Part IV is sent to downstream process as washing lotion；
This step prevailing operating conditions：
IV section of flashing operation temperature：-73℃
IV section of flashing operation pressure：0.3bar.
Embodiment 3
The method that a kind of solution circular regeneration in the present embodiment improves recovery rate of CO 2 and purity, including following step
Suddenly：
(1)CO2It absorbs
Raw gas is removed into H by hydrogen sulfide absorption tower first2Element sulphur in S and COS, from hydrogen sulfide absorption tower
Desulfurization rough coal throughput is 200000Nm3/ h, temperature：- 12 DEG C, pressure：60bar, the specific gas group of sweet gas become：
| Composition | H2 | N2 | CO | CH4 | CO2 | ∑ |
| V% | 41.6 | 0.79 | 19.0 | 12.61 | 26.0 | 100.0 |
Then enter CO2Absorption tower 1, methanol lean solution is from CO2Absorption tower 1 tower top sprays into, and from CO21 bottom of tower of absorption tower enters
Sweet gas counter current contacting, in CO2Carbon dioxide eliminating is carried out in absorption tower 1, from CO2Solution is drawn through two in 1 middle part of absorption tower
Ammonia cooler 2,3 returns to CO after cooling down2Improving CO in absorption tower 12Solubility, CO21 epimere of absorption tower is introduced through flash column
Half poor methanol liquid after vacuum flashing is improving CO2Uptake, carbon content reaches 10ppm in purified gas, purifies
Gas afterwards is from CO21 tower top of absorption tower leaves, into downstream process, CO2The rich carbon methanol solution one of 1 bottom of tower of absorption tower outflow
To hydrogen sulfide absorption tower as desulfurization washing lotion, another part is sent to flash column to regenerated methanol, while recycling CO for dispensing2As
Product gas；
In CO2When absorption tower 1 carries out carbon dioxide eliminating, since absorption process can discharge heat of solution, methanol solution temperature
It can rise therewith, lead to the reduction of Solubilities of Carbon Dioxide, it is therefore desirable in CO2It is molten that absorption is drawn at 1 intermediate tray of absorption tower
Liquid returns to CO after two ammonia coolers 2, the cooling of 3 ammonia2To improve CO in 1 tower of absorption tower2Solubility, in CO2Absorption tower 1 it is upper
Section then introduces half poor methanol solution after vacuum flashing, to improve CO2Uptake, purified gas is from CO21 tower of absorption tower
It is lifted off out, into downstream process, absorption has CO2Rich carbon methanol solution then a part is sent to hydrogen sulfide absorption tower and is washed as desulfurization
Liquid, another part is then sent to flash evaporation unit with regenerated methanol, while recycling CO2As product gas.
This step prevailing operating conditions：
CO2Absorption tower operation temperature：-12℃
CO2Absorption tower operating pressure：60bar
(2) I sections of flash distillations and absorption
From CO2The rich carbon methanol solution on absorption tower 1 is sent after decompression to I section of flash vessel 4 positioned at flash distillation tower bottom,
Rich carbon methanol solution is flashed from the middle part of I section of flash vessel 4 into I section of flash vessel 4, H2、N2、CO、Ar、CH4Inertia group self-dissolving
It is flashed off in liquid, due to CO2Solubility is more than above-mentioned inert component, therefore CO2It can stay in rich carbon methanol solution, I section of flash distillation
One of 4 epimere of device introducing washs vapor phase from half poor methanol after the flash distillation of IV section of flash vessel 7 of flash column, to ensure
CO2The rate of recovery, the steaming liquid come out from I section of 4 bottom end of flash vessel mutually sent under the action of itself pressure difference to II section of sudden strain of a muscle of flash column
Steaming device 5, the flashed vapour come out from I section of 4 top of flash vessel go to compress to be back in unstripped gas to recycle, I section of flash distillation gas phase stream
Amount is 2804Nm3/h；
I section of flash distillation and absorption operation temperature：-26℃；
I section of flash distillation and absorption operation pressure：15bar；
(3) II sections of flash distillations and absorption
Contain CO by I section of flash vessel 42Methanol solution enters II section of flash vessel 5 being located at the top of flash column, part CO2Quilt
It flashes off, and battery limit (BL) is sent out from flash column top export after the half poor methanol solution washing from IV section of flash vessel 7, it should
The CO that section flashes off2Flow is 17500Nm3/ h, purity 95.4%mol, CO2Purity of product gas reaches 95% or more, flash distillation
Afterwards contain CO2Methanol solution be then sent to III section of flash vessel 6 of flash column and continue to flash,；
II section of flash distillation and absorption operation temperature：-48℃；
II section of flash distillation and absorption operation pressure：3.0bar；
(4) III sections of flash distillations
Contain CO by what II section of flash vessel 5 flashed2Methanol solution enters III section of flash vessel for being located at II section of 5 lower section of flash vessel
It is flashed in 6, the CO flashed off2Product comes out from III section of flash vessel 6, obtains CO2Product throughput is
18000Nm3/ h, purity 99.4%mol, since the flash process of carbon dioxide can absorb heat, operation temperature can be into
One step reduces, and contains CO after flash distillation2Methanol solution be then sent to IV section of flash vessel 7 and continue to flash；
III section of flash distillation and absorption operation temperature：-60℃；
III section of flash distillation and absorption operation pressure：0.9bar；
(5) IV sections of flash distillations
Contain CO by III section of flash vessel 62Methanol solution enters in IV section of flash vessel 7 for being located at III section of 6 lower section of flash vessel
It is flashed, the CO flashed off at this time2Product comes out from IV section of flash vessel 7, obtains CO2Product throughput is
8500Nm3/ h, purity 99.8%mol, half poor methanol after flash distillation are divided into four parts, and first part send through pump 8 to CO2It absorbs
1 epimere of tower is as absorption CO2It recycles, second part send to I section of flash vessel 4 through pump 10 and recycles, and Part III is through pump 9
It send to II section of flash vessel 5 and recycles, Part IV is sent to downstream process as washing lotion；
This step prevailing operating conditions：
IV section of flashing operation temperature：-70℃；
IV section of flashing operation pressure：0.4bar.
Claims (6)
1. a kind of method that solution circular regeneration improves recovery rate of CO 2 and purity, it is characterised in that：Include the following steps：
(1)CO2It absorbs
The raw gas that pressure is 3.0~6.0Mpa is removed into H by hydrogen sulfide absorption tower first2Element sulphur in S and COS, then
Into CO2Absorption tower (1), methanol lean solution is from CO2Absorption tower (1) tower top sprays into, and from CO2The desulfurization that absorption tower (1) bottom of tower enters
Gas counter current contacting, in CO2Carbon dioxide eliminating is carried out in absorption tower (1), from CO2Solution is drawn in the middle part of absorption tower (1) through two ammonia
CO is returned after cooler (2,3) is cooling2Improving CO in absorption tower (1)2Solubility, CO2Absorption tower (1) epimere is introduced through dodging
Half poor methanol liquid after tower vacuum flashing is steamed to improve CO2Uptake, purified gas is from CO2Absorption tower (1) tower top from
It opens, into downstream process, CO2A rich carbon methanol solution part for absorption tower (1) bottom of tower outflow is sent to hydrogen sulfide absorption tower conduct
Desulfurization washing lotion, another part is sent to flash column to regenerated methanol, while recycling CO2As product gas；
(2) I sections of flash distillations and absorption
From CO2The rich carbon methanol solution on absorption tower (1) is sent after decompression to I section of flash vessel (4) positioned at flash distillation tower bottom,
Rich carbon methanol solution is flashed from the middle part of I section of flash vessel (4) into I section of flash vessel (4), H2、N2、CO、Ar、CH4Inertia group
It is flashed off from solution, due to CO2Solubility is more than above-mentioned inert component, therefore CO2It can stay in rich carbon methanol solution, I section
One of flash vessel (4) epimere introducing washs gas phase from half poor methanol after the flash distillation of IV section of flash vessel (7) of flash column, to
Ensure CO2The rate of recovery, the steaming liquid come out from I section of flash vessel (4) bottom end mutually send under the action of itself pressure difference to flash column
II section of flash vessel (5), the flashed vapour come out from I section of flash vessel (4) top go to compress to be back in unstripped gas to recycle；
(3) II sections of flash distillations and absorption
Contain CO by I section of flash vessel (4)2Methanol solution enters II section of flash vessel (5) being located at the top of flash column, part CO2Quilt
It flashes off, and battery limit (BL) is sent out from flash column top export after the half poor methanol solution washing from IV section of flash vessel (7),
Contain CO after flash distillation2Methanol solution be then sent to III section of flash vessel (6) of flash column and continue to flash；
(4) III sections of flash distillations
Contain CO by what II section of flash vessel (5) flashed2Methanol solution enters III section of flash vessel being located at below II section of flash vessel (5)
(6) it is flashed in, the CO flashed off2Product comes out from III section of flash vessel (6), contains CO after flash distillation2Methanol solution
IV section of flash vessel (7) is then sent to continue to flash；
(5) IV sections of flash distillations
Contain CO by III section of flash vessel (6)2Methanol solution enters in IV section of flash vessel (7) being located at below III section of flash vessel (6)
It is flashed, the CO flashed off at this time2Product comes out from IV section of flash vessel (7), and half poor methanol after flash distillation is divided into four
Part, first part send through pump (8) to CO2Absorption tower (1) epimere is as absorption CO2It recycles, second part is sent through pump (10)
Recycled to I section of flash vessel (4), Part III send to II section of flash vessel (5) through pump (9) and recycles, remaining part send to
Downstream process is as washing lotion；
2. the method that a kind of solution circular regeneration according to claim 1 improves recovery rate of CO 2 and purity, special
Sign is：CO in the step (1)2Absorption tower unstripped gas temperature：- 12~-30 DEG C；Carbon dioxide absorption tower operating pressure：30
~60bar.
3. the method that a kind of solution circular regeneration according to claim 1 improves recovery rate of CO 2 and purity, special
Sign is：I section of flash distillation and absorption operation temperature in the step (2)：- 26~-31 DEG C；I section of flash distillation and absorption operation pressure：9
~15bar.
4. the method that a kind of solution circular regeneration according to claim 1 improves recovery rate of CO 2 and purity, special
Sign is：II section of flash distillation and absorption operation temperature in the step (3)：- 48~-53 DEG C；II section of flash distillation and absorption operation pressure：
1.4~3.0bar.
5. the method that a kind of solution circular regeneration according to claim 1 improves recovery rate of CO 2 and purity, special
Sign is：III section of flashing operation temperature in the step (4)：- 60~-65 DEG C；III section of flashing operation pressure：0.5~0.9bar.
6. improving the side of recovery rate of CO 2 and purity according to a kind of solution circular regeneration of claim 1-5 any one of them
Method, it is characterised in that：IV section of flashing operation temperature in the step (5)：- 70~-75 DEG C；IV section of flashing operation pressure：0.25
~0.4bar.
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| CN101885993A (en) * | 2010-07-12 | 2010-11-17 | 赛鼎工程有限公司 | Purification process for removing sulphur and carbon dioxide in gas by using two-step method |
| JP2011168628A (en) * | 2010-02-16 | 2011-09-01 | Hitachi Ltd | Gas purification method and gas purification device |
| CN103320176A (en) * | 2013-06-20 | 2013-09-25 | 华南理工大学 | A low-temperature methanol washing method and device with high CO2 yield |
| CN105542876A (en) * | 2015-12-15 | 2016-05-04 | 七台河宝泰隆煤化工股份有限公司 | Method for using low temperature methanol washing apparatus for removal of impurities in shift gas |
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| JP2011168628A (en) * | 2010-02-16 | 2011-09-01 | Hitachi Ltd | Gas purification method and gas purification device |
| CN101885993A (en) * | 2010-07-12 | 2010-11-17 | 赛鼎工程有限公司 | Purification process for removing sulphur and carbon dioxide in gas by using two-step method |
| CN103320176A (en) * | 2013-06-20 | 2013-09-25 | 华南理工大学 | A low-temperature methanol washing method and device with high CO2 yield |
| CN105542876A (en) * | 2015-12-15 | 2016-05-04 | 七台河宝泰隆煤化工股份有限公司 | Method for using low temperature methanol washing apparatus for removal of impurities in shift gas |
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