CN101745288A - Method for vacuum pressure and temperature varying coupling adsorbing and trapping carbon dioxide in flue gas - Google Patents
Method for vacuum pressure and temperature varying coupling adsorbing and trapping carbon dioxide in flue gas Download PDFInfo
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- CN101745288A CN101745288A CN201010023008A CN201010023008A CN101745288A CN 101745288 A CN101745288 A CN 101745288A CN 201010023008 A CN201010023008 A CN 201010023008A CN 201010023008 A CN201010023008 A CN 201010023008A CN 101745288 A CN101745288 A CN 101745288A
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- 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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- 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
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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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
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention relates to a trapping method of carbon dioxide, namely a method for multi-tower vacuum pressure and temperature varying coupling adsorbing and concentrating the carbon dioxide. The method comprises the following main steps: (a) under the conditions of 10-50 DEG C of temperature and 1.1-5.0 atm of pressure, adopting an adsorbent for adsorbing the carbon dioxide to adsorb the carbon dioxide in flue gas; (b) under the conditions of 80-150 DEG C of temperature and 1-10 kPa of vacuum, desorbing the adsorbent in step (a), and cooling the obtained gas containing the carbon dioxide to enter a gas collector. The method has the advantages that under the auxiliary condition of heating temperature rising, the adsorbent is desorbed in vacuum, and the power consumption and the cost of vacuum equipment are reduced; pipe-shell absorbers or the absorbers of enhanced heat transfer elements of tower inbuilt fin type, coils, and the like to increase the indirect heating and cooling efficiency; and adopting low-temperature exhaust gas discharged from the top end of an adsorption tower to directly regenerate a post adsorbent in a bed to shorten the cooling time. Compared with the prior art, the method reduces the trapping and post processing cost of the carbon dioxide.
Description
Technical field
The present invention relates to the capture method of a kind of carbon dioxide (greenhouse gases), specifically, is the method that a kind of vacuum pressure and temperature varying coupling captures carbon dioxide in the flue gas.
Background technology
The 4th part of report that the Intergovernmental Panel on Climate Change of UNEP (United Nations Environment Program) (IPCC) delivers at the beginning of 2007 points out that climate warming has been the mathematical fact, and the possibility more than 90% is that mankind's activity has caused climate change.Since industrialization,, during 1970 to 2004, increased by 70%, carbon dioxide (CO in the global atmosphere because the global greenhouse gas emission that mankind's activity produced has increased
2) concentration has been increased to 379ppm in 2005, and has been discharged into the CO of atmosphere by about 280ppm in epoch before the industrialization
23/4 cause by combustion of fossil fuel.According to the prediction of USDOE, the annual in the world necessary CO that reduces 6,000,000,000 tons
2Discharging could really prevent Global climate change.Reach with energy-saving and cost-reducing, exploitation regenerative resource etc. except employing new technology and to reduce discharging the purpose, the technology (CCS) of catching and seal up for safekeeping of carbon dioxide has and wholely reduces cost and increase the potentiality that realize the reduction of greenhouse gas discharge flexibility.
Capture CO
2Main method absorption process, absorption method, membrane separation process and low temperature processing are arranged.Wherein absorption process and absorption method have longer history, are used for industrial process such as oil refining, synthetic ammonia, hydrogen manufacturing, natural gas purification in a large number, and be relatively ripe, has a large amount of experiences can reference.Chemical absorbing that it is generally acknowledged amine solvent is CO in the flue gas of discharging such as capturing power plant, steel mill
2The method that application prospect is relatively arranged is with the CO after MEA (MEA) the absorption burning
2Be reference, its energy consumption is 4.2～4.8MJ/kgCO
2, the CO in capturing middle-size and small-size power plant, steel mill and cement plant flue gas
2The time, absorption method is simple because of its equipment, energy consumption is low, easily be automated operation, needn't consider that corrosion problems etc. has bigger advantage.Along with the exploitation of new and effective adsorbent and the optimization of separation process technique, absorption method captures CO
2Cost can descend significantly, make this technology have competitiveness.
Although all comprise adsorbing and removing CO at industrial process such as synthetic ammonia, hydrogen manufacturing, natural gas purifications
2Operation, yet by capturing separation of C O in power plant, steel mill, the cement plant flue gas
2Have significantly differently with these processes, this mainly is the character decision of pending system.Flue gas has following characteristics: (1) gas flow is very big, and nearly normal pressure; (2) CO
2Dividing potential drop lower (3%～20%); (3) after the waste heat recovery, about 100 ℃～150 ℃ of effluent gas temperature; (4) contain a large amount of inert gas N
2(more than 70%); (5) contain H
2O, SO
2, impurity such as NOx.Many normal temperature carbon dioxide absorbing material and technology (as natural zeolite, molecular sieve, silica gel, active carbon, mesoporous material, metal-organic framework materials etc.) and high temperature carbon dioxide sorbing material and technologies (as hydrotalcite, metal oxide, lithium salts and calcium oxide) of being applicable to are arranged.But when being used for catching the flue gas carbon dioxide, existing adsorption separation technology operating cost is still higher, differs greatly with the carbon dioxide capture cost of expecting.
Novel absorption material is as amido mesoporous material, 13X-APG zeolite, 13X-APG-IIA zeolite etc., to low concentration CO
2Adsorption capacity bigger, but vacuum desorption pressure is very low, the vavuum pump energy consuming ratio is higher.It also is higher adopting traditional alternating temperature adsorbing and trapping cost and energy consumption.
Given this, this area presses for carbon dioxide method in a kind of novel capture flue gas, overcomes the CO that exists in the prior art
2Adsorbing and trapping cost and energy consumption are higher, and because the CO that is captured
2Defectives such as post processing (pressurization is sealed up for safekeeping) the cost rising that purity not high (being less than or equal to 75v/v%) causes.
Summary of the invention
The present invention adopts CO in novel absorption material (amido mesoporous material, 13X-APG zeolite, 13X-APG-IIA zeolite) the adsorbing and trapping flue gas
2, the method that provides a kind of tower vacuum pressure and temperature varying to be coupled capturing carbon dioxide.This trapping technique also is applicable to other sorbing material, as natural zeolite, NaX, NaY, 5A zeolite molecular sieve, silicon titanium molecular sieve, mesoporous material, metal-organic framework materials, silica gel, activated alumina and active carbon etc.
The method of carbon dioxide comprises the following steps: in the capture flue gas of the present invention
(a) be 10 ℃～50 ℃ in temperature, pressure is under 1.1 atmospheric pressure (atm)～5.0atm condition, adopts the existing adsorbents adsorb flue gas carbon dioxide that is used for absorbing carbon dioxide;
(b) be that 80 ℃～150 ℃ and vacuum are that (preferred vacuum is: under the condition of 3kPa～6kPa), the adsorbent in the step (a) is resolved, the carbon dioxide containing gas of resolving gained enters gas collector to 1kPa～10kPa after cooling in temperature.
Wherein: described adsorbent is selected from: one or two or more kinds in 13X-APG zeolite, 13X-APG-IIA zeolite, 5A molecular sieve, amido mesoporous material, NaX, NaY zeolite, silicon titanium molecular sieve, mesoporous material, metal-organic framework materials, silica gel, activated aluminum or the material with carbon element;
The content of carbon dioxide is 3v/v%～20v/v% in the described flue gas (from the flue of power plant, steel mill and cement plant discharging), and the content of nitrogen is about 70v/v%, and surplus is sulfur dioxide (SO
2) gas, nitrogen oxygen (NOx) gas and steam etc.
Description of drawings
The block diagram of Fig. 1 eight step vacuum pressure and temperature varying (VPTSA) coupling absorbing process cyclings;
The process chart of Fig. 2 four towers eight step vacuum pressure and temperature varying coupling adsorbing and trapping carbon dioxide.
Wherein: be followed successively by adsorption tower 1, adsorption tower 2, adsorption tower 3 and adsorption tower 4 from left to right; The control regulation valve function declaration sees Table 1 separately
Table 1
The specific embodiment
The method that below provides a kind of multi-tower type vacuum pressure and temperature varying of the present invention coupling absorption to concentrate carbon dioxide, its mainly by adsorb, all press, intensification, vacuum, vacuum eight steps that purge, all press, pressurize, lower the temperature form, and are specific as follows:
Step (1) absorption:
In temperature is that 10 ℃～50 ℃, pressure are under 1.1atm～5atm condition, carbon dioxide in adsorbing and trapping flue gas or the industrial manufacture process discharge tail gas, its CO
2Concentration is at 3v/v%～30v/v%; This operating procedure is introduction of use CO also
2The follow-up further cooled feed gas body of the low-grade cold that waits other technology of sealing up for safekeeping.Adopt cold burden to adsorb, improve adsorbing and trapping CO
2Can also cool off adsorbent in forward's adsorbent bed in the time of ability, shorten the middle adsorbent of step (8) and lower the temperature cool time, increase productivity;
Described adsorbent is selected from 13X-APG zeolite, 13X-APG-IIA zeolite, 5A molecular sieve, amido mesoporous material, NaX, NaY zeolite, silicon titanium molecular sieve, mesoporous material, metal-organic framework materials, silica gel, one or several in activated aluminum or the material with carbon element;
Step (2) is all pressed: all press with another vacuum low-pressure absorber step (6), comprise reverse or oppositely all press; Carry out step (2) operating procedure absorber pressure and drop to normal pressure; Also discharge the weak absorbed component nitrogen in the adsorbent bed when all pressing, CO in the product gas that the raising desorb obtains
2Purity;
Step (3) heats up: the indirect adsorbent carries out desorb, adds heat-adsorbent by heat medium or energising, makes the interior adsorbent temperature of absorber rise to 80 ℃～150 ℃; The CO that heating desorption goes out
2Gas enters the product gas tank and reclaims after cooling;
Enhanced heat transfer components such as adsorbent bed inbuilt fin type also can use the shell-and-tube absorber, improve indirect efficient;
Described heating thermal source is the low-grade waste heat of other technology of factory; Heat medium may be saturated or superheated vapour, the gas of heat or the liquid of heat; The heat medium temperature is 100 ℃～200 ℃;
Step (4) vacuum: vacuum desorption, vacuum pressure 1kPa～10kPa; Comprise reverse or oppositely vacuumize; Separate the CO of sucking-off
2Gas enters the product gas tank and reclaims after cooling;
Step (5) vacuum purges: the carbon dioxide that retains in the reverse product air-blowing eroding river bed, separate the CO of sucking-off
2Gas enters the product gas tank and reclaims after cooling; This purge gas also can comprise other carrier gas such as nitrogen, but used in amounts will be controlled CO in the assurance product gas
2Purity.
Step (6) is all pressed: all press with the step (2) of the higher absorber of another pressure, save the power consumption of conveying equipment; Because it is lower to carry out the interior temperature of step (2) operating procedure absorber, temperature is 10 ℃～50 ℃, also carries out the adsorbent cooling simultaneously so the absorber of step (6) operating procedure is all pressed;
Step (7) pressurization: the pressure when adopting flue gas to be forced into absorption in the bed, if use cold flue gas pressurization, absorber also carries out the adsorbent cooling simultaneously;
Step (8) cooling: directly, indirectly or directly cool off adsorbent in the adsorbent bed indirectly simultaneously; Reverse directly by the adsorption tower step (8) after the regeneration by another packed bed outflow tail gas that carries out step (1) adsorbing and trapping, directly the interior adsorbent of cooling tower adopts the cooling of cooling medium secondary indirect adsorbent bed in case of necessity, shortens cool time; When temperature drops to 50～60 ℃ in the bed, shut-down operation; When being recycled to next operating procedure (1), adopt cold burden to adsorb, in the time of raising adsorbing and trapping efficient, also continue cooling adsorbent bed inside forward's adsorbent simultaneously, the control operation condition, adsorption capacity can not descend when guaranteeing effectively to cool off adsorbent.
Described direct cooling medium is served as reasons, and another carries out the low temperature exhaust gas of packed bed outflow of step (1) adsorbing and trapping; Cryogenic gas, liquid that described indirect cooling medium is air, water, other technology, coolant temperature are 0 ℃～30 ℃; The low-temperature receiver that provides comprises and utilizes follow-up CO
2The cold of compression section;
In the whole circulation adsorption/desorption technology, coupling desorption pressures 1kPa～10kPa, 80 ℃～150 ℃ of desorption temperatures are embodied in step (3), (4), (5); The auxiliary about 0-30 degree of indirect coolant temperature is embodied in the step (8); Feeding refrigerating gas directly cools off in the present step of sorbent body (6), (7), (8), (1); Utilize follow-up CO
2The cold of compression section is embodied in step (1), (8).
The continuous adsorption capturing carbon dioxide need adopt a plurality of adsorption tower parallel work-flows, and Fig. 2 shows that a typical case four towers eight step vacuum pressure and temperature varying coupling technique continuous adsorption capture CO
2Operating process, each valve function and mode of operation are as shown in table 1; Eight operating procedures of each circulation are divided into four equal time periods, (1) adsorption time section, all press and the heating-up time section (2), (3) vacuum, purging, all press and pressing time section, (4) temperature fall time section.Traditional temperature swing adsorption process temperature fall time is longer, and the adsorption time section also is another temperature fall time section in this technological design, and in fact the present invention adopts two temperature-fall periods (step (8) temperature-fall period and step (1) absorption phase).But, need optimal design to guarantee that the absorption forward should be slower than the heat wave peak and could improve cooling efficient in the adsorption time section.
The mode of operation of four towers is as shown in table 2, and adsorption tower 1 adsorbs, and adsorption tower 2 is lowered the temperature, and adsorption tower 3 carries out vacuum, purging, all presses and pressurizes, and adsorption tower 4 is all pressed and heated up; Sequencing valve is controlled automatically, and next time period, adsorption tower 1 is all pressed and heated up, and adsorption tower 2 adsorbs, and adsorption tower 3 is lowered the temperature, and adsorption tower 4 carries out vacuum, purging, all presses and pressurizes; Then sequencing valve is regulated again automatically, and each adsorption tower carries out next mode of operation, and adsorption tower 1 carries out vacuum, purging, all presses and pressurizes, and adsorption tower 2 is all pressed and heated up, and adsorption tower 3 adsorbs, and adsorption tower 4 is lowered the temperature; Sequencing valve is regulated automatically again, and at this moment, adsorption tower 1 is lowered the temperature, and adsorption tower 2 carries out vacuum, purging, all presses and pressurizes, and adsorption tower 3 is all pressed and heated up, and adsorption tower 4 adsorbs.By the automatic adjusting of sequencing valve, each adsorption tower will repeat aforesaid operations, and this technology can guarantee the continuous adsorption capturing carbon dioxide.
Table 2
Compared with prior art, good effect of the present invention is:
Compare with traditional Vacuum Pressure Swing Adsorption technology, the present invention's first concrete scheme is to add the alternating temperature adsorption technology, and vacuum desorption adsorbent under the heat temperature raising subsidiary conditions is because heating can make CO
2Desorb easilier, thereby reduced the power consumption of vavuum pump from adsorbent; Adopt above-mentioned adsorbent, auxiliary desorb heating-up temperature is not that requirement is very high, be about 80～150 ℃, can both make adsorbent reach regeneration rate more than 80%, the heating thermal source can adopt the unemployed low grade residual heat of factory like this, whole technology operation is more economical, and energy consumption and vacuum equipment cost all can significantly descend.
Longer at the alternating temperature adsorption time, can reduce the weakness of production capacity, the present invention's second concrete scheme improves the alternating temperature adsorption efficiency.Enhanced heat transfer components such as shell-and-tube absorber or adsorbent bed inbuilt fin type are adopted in one of measure, improve indirect and cooling effectiveness, shorten the heating and cooling time, increase productivity; Two of measure, adsorbent cools and carries out in two stages, phase I mainly occurs in temperature fall time section (step (8)), and the low temperature exhaust gas that adopts the adsorption tower top to discharge directly passes through regeneration back tower cooler cooling sorbing material, adds indirect auxiliary cooling system in case of necessity; Second stage temperature descending section generation absorption phase (step (1)) adopts cold burden to enter adsorption tower absorption, and cooling forward's adsorption bed in the time of absorption keeps the adsorbing and trapping rate, about 20 ℃ or lower slightly again of the temperature of cold burden; Three of measure, the low-temperature receiver of cooling charging can utilize compresses low-grade cold of sealing up for safekeeping in the technology, and the indirect medium adopts the unemployed low grade residual heat of factory, cuts down the consumption of energy.
In addition, adopt more than the purity 90v/v% of the resulting carbon dioxide of capturing carbon dioxide method of the present invention, do not need further to carry dense, can directly be compressed to 100 atmospheric pressure, condensation liquefaction, discharging fixed gas after, seal up for safekeeping, reduce the cost of the post processing of capturing carbon dioxide.
Below by embodiment content of the present invention is further elaborated, its purpose only is better to understand content of the present invention.
Embodiment 1
Adopt the experiment example of carbon dioxide in the vacuum pressure and temperature varying coupling technique absorption flue gas, the experiment of single-column comprises absorption, heats, vacuumizes, vacuum purges, cool cycles capture CO
2Step.116 gram 13X APGIIA zeolites are filled in the stainless steel tube that internal diameter is 25mm, and packed height is 350mm.The 13X-APGIIA zeolite adsorbents is that global molecular sieve Co., Ltd buys from Shanghai, aperture 10A, and particle size is about 2.0mm.This absorber is designed to jacket type, and interior pipe is filled adsorbent, and chuck admittance deep fat is so that adsorbent in the heating and cooling absorber, and the temperature of circulating heat conduction oil is controlled by the high and low temperature constant temperature bath.
Simulated flue gas (15%CO
2And 85%N
2) entering adsorption tower at the bottom of by tower under nearly normal pressure (1.33atm) and the normal temperature (30 ℃), eluting gas is respectively through chromatogram and CO on a small quantity
2The online detection of infrared in-line analyzer CO
2Concentration is to adsorption bed 30% breakthrough.Begin to adopt 100～180 ℃ of heat-conducting oil heating adsorbent beds, be warmed up to 80～150 ℃ regeneration temperature.Start vavuum pump, carry out reverse vacuum desorption, to vacuum pressure be 3kPa～6kPa.Flow integrator metering vacuum desorption product tolerance, CO in the online detection desorb of the infrared in-line analyzer product gas
2Concentration.Again under vacuum condition, with the CO of retention in the reverse purging packed bed of a spot of nitrogen
2Behind the adsorbent reactivation, pressurization, and with 10 ℃～20 ℃ conduction oils indirectly cooling and normal temperature nitrogen directly cool off adsorbent bed to 50 ℃ simultaneously by bed, prepare the next circulation of beginning and adsorb/take off suction and operate.The whole circulation time is about 20 minutes～and 30 minutes, behind the stable circulation, record the adsorbent reactivation rate and reach more than 90% CO
2The rate of recovery reaches more than 90%.Product tolerance is about 0.10～0.15 kilogram of (CO
2(adsorbent) (each circulation) of)/kilogram is two to four times of conventional Vacuum Pressure Swing Adsorption handicraft product tolerance, and CO in the product gas
2Purity can reach more than the 90v/v%, can directly be compressed to 100 atmospheric pressure, removes fixed gas, seals up for safekeeping underground.And conventional Vacuum Pressure Swing Adsorption technology, the about 65v/v%～75v/v% of purity of product gas need further carry concentrated.
The above only is a preferred implementation of the present invention; should be pointed out that for those skilled in the art, without departing from the inventive concept of the premise; can also make some improvements and modifications, these improvements and modifications also should be considered within the scope of protection of the present invention.
Claims (9)
1. a method that captures carbon dioxide in the flue gas comprises the following steps:
(a) be 10 ℃～50 ℃ in temperature, pressure is under 1.1atm～5.0atm condition, adopts the existing adsorbents adsorb flue gas carbon dioxide that is used for absorbing carbon dioxide;
(b) be that 80 ℃～150 ℃ and vacuum are under the condition of 1kPa～10kPa in temperature, the adsorbent in the step (a) resolved that the carbon dioxide containing gas of resolving gained enters gas collector after cooling.
2. the method for claim 1 is characterized in that, the vacuum in the step (b) is 3kPa～6kPa.
3. method as claimed in claim 1 or 2, it is characterized in that wherein said adsorbent is selected from: one or two or more kinds in 13X-APG zeolite, 13X-APG-IIA zeolite, 5A molecular sieve, amido mesoporous material, NaX, NaY zeolite, silicon titanium molecular sieve, mesoporous material, metal-organic framework materials, silica gel, activated aluminum or the material with carbon element.
4. method as claimed in claim 3 is characterized in that, described method is the method that a kind of multi-tower type vacuum pressure and temperature varying coupling absorption concentrates carbon dioxide, and it is circulation absorption and desorption technique process; Each circulation comprises absorption, all presses, intensification, vacuum, vacuum purge, all press, pressurize and lower the temperature eight steps; Its concrete steps are:
Step (1) absorption: in temperature is that 10 ℃～50 ℃, pressure are under 1.1atm～5atm condition, carbon dioxide in adsorbing and trapping flue gas or the industrial manufacture process discharge tail gas, its CO
2Concentration is at 3v/v%～30v/v%;
Step (2) is all pressed: all press with another vacuum low-pressure absorber step (6), comprise reverse or oppositely all press; Carry out step (2) operating procedure absorber pressure and drop to normal pressure;
Step (3) heats up: the indirect adsorbent carries out desorb, makes the interior adsorbent temperature of absorber rise to 80 ℃～150 ℃; The CO that heating desorption goes out
2Gas enters the product gas tank and reclaims after cooling;
Step (4) vacuum: vacuum desorption, vacuum pressure 1kPa～10kPa; Comprise reverse or oppositely vacuumize; Separate the CO of sucking-off
2Gas enters the product gas tank and reclaims after cooling;
Step (5) vacuum purges: the carbon dioxide that retains in the gas purging beds such as reverse product gas, separate the CO of sucking-off
2Gas enters the product gas tank and reclaims after cooling;
Step (6) is all pressed: all press with the step (2) of the higher absorber of another pressure;
Step (7) pressurization: the pressure when adopting flue gas to be forced into absorption in the bed;
Step (8) cooling: reverse directly by the adsorption tower step (8) after the regeneration by another packed bed outflow low temperature exhaust gas that carries out step (1) adsorbing and trapping, adsorbent in the direct cooling tower, adopt the cooling of cooling medium secondary indirect adsorbent bed in case of necessity, shorten cool time; When temperature drops to 50 ℃～60 ℃ in the bed, shut-down operation; Be recycled to next operating procedure (1).
5. method as claimed in claim 4 is characterized in that wherein enhanced heat transfer components such as adsorbent bed inbuilt fin chip, coil pipe also can use the shell-and-tube absorber, improves indirect and cooling effectiveness;
In step (1), go back introduction of use CO
2Subsequent compression is sealed the further cooled feed gas body of the low-grade cold that waits other technology up for safekeeping.Adopt cold burden to adsorb, improve adsorbing and trapping CO
2Can also cool off adsorbent in forward's adsorbent bed in the time of ability, shorten the middle adsorbent of step (8) and lower the temperature cool time.
6. method as claimed in claim 4 is characterized in that, in step (3):
Add heat-adsorbent by indirect medium or energising and carry out adsorbent reactivation, adsorbent temperature rises to 80 ℃～150 ℃;
Described heating thermal source is the low-grade waste heat of other technology of factory; Heat medium may be saturated or superheated vapour, the gas of heat or the liquid of heat; The heat medium temperature is 100 ℃～200 ℃;
When adsorbent has the favorable conductive heat conductivility,, can consider to adopt energising directly to add heat-adsorbent and cut down the consumption of energy if lack the low-grade waste heat of factory.
7. method as claimed in claim 4 is characterized in that, in step (5):
Adopt the carbon dioxide that retains in the product air-blowing eroding river bed, improve CO in the product gas
2Purity; This purge gas also can comprise other carrier gas such as nitrogen, but used in amounts will be controlled CO in the assurance product gas
2Purity.
8. method as claimed in claim 4 is characterized in that, in step (8) and step (1):
Divide two sections to carry out the adsorbent bed cooling;
The first temperature fall time section occurs in step (8), reverse by another packed bed outflow low temperature exhaust gas that carries out step (1) adsorbing and trapping directly by the adsorption tower step (8) after the regeneration, adsorbent in the direct cooling tower, adopt the cooling of cooling medium secondary indirect adsorbent bed in case of necessity, shorten cool time; When temperature drops to 50 ℃～60 ℃ in the bed, shut-down operation;
The second temperature fall time section occurs in step (1), adopts cold burden to adsorb, and in the time of raising adsorbing and trapping efficient, also continues cooling adsorbent bed inside forward's adsorbent simultaneously, the control operation condition, and adsorption capacity can not descend when guaranteeing effectively to cool off adsorbent;
Described direct cooling medium is served as reasons, and another carries out the low temperature exhaust gas of packed bed outflow of step (1) adsorbing and trapping; Cryogenic gas, liquid that described indirect cooling medium is air, water, other technology, coolant temperature are 0 ℃～30 ℃; The low-temperature receiver that provides comprises and utilizes follow-up CO
2The cold of workshop section is sealed in compression up for safekeeping.
9. method as claimed in claim 4 is characterized in that, whole circulation technology improves adsorbent rate of temperature fall in the absorber by following measure:
Feeding refrigerating gas directly cools off in the present step of sorbent body (6), (7), (8), (1); About 0 ℃～30 ℃ of auxiliary indirect coolant temperature is embodied in the step (8); Utilize follow-up CO
2The cold of compression section is embodied in step (1), (8); Enhanced heat transfer components such as adsorbent bed inbuilt fin chip, coil pipe also can use the shell-and-tube absorber, improve indirect cooling effectiveness.
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| CN1872389A (en) * | 2006-04-28 | 2006-12-06 | 上海申江化肥成套设备有限公司 | Technique for adsorption under live pressure, and equipment |
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