CN101218011A - Method for the removal of trace components by adsorption - Google Patents
Method for the removal of trace components by adsorption Download PDFInfo
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- CN101218011A CN101218011A CNA2006800249836A CN200680024983A CN101218011A CN 101218011 A CN101218011 A CN 101218011A CN A2006800249836 A CNA2006800249836 A CN A2006800249836A CN 200680024983 A CN200680024983 A CN 200680024983A CN 101218011 A CN101218011 A CN 101218011A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40067—Seven
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40073—Ten
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40058—Number of sequence steps, including sub-steps, per cycle
- B01D2259/40075—More than ten
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
A method is described for the removal by adsorption of at least one component (trace component) present in a concentration of less than 2% by volume from a gas mixture having at least two further components (main components). This method has the following method steps according to the invention: a) feeding the crude gas at adsorption pressure, adsorption of the trace component to the adsorption medium and removal of product gas, b) heating the laden adsorption medium using a regeneration gas which has a higher temperature than the crude gas fed to the adsorber during the adsorption, which regeneration gas is provided by a regeneration gas source and which after passage through the adsorber is fed to a regeneration gas remover, and c) batchwise or continuous flow of crude and/or product gas through the adsorption medium for a period of at least 30 minutes, in which case this gas stream or gas streams, after flow through the adsorption medium, is or are fed to the regeneration gas remover and the quantitative flow rate is at most 7% of the crude or product gas flow rate fed or removed during method step a).
Description
Technical field
The present invention relates to a kind of method that at least a composition that exists with the concentration less than 2% volume ratio (trace constituent) is removed on the method that realizes by means of the absorber that is arranged in parallel at least two absorption ground from a kind of admixture of gas with at least two kinds of other compositions (principal component) that is used for.
Be interpreted as any adsorbing medium of forming by one or more materials (mixing bed) for described notion " adsorbing medium ".
Be so basically in having the admixture of gas of multiple principal component, that is, these principal components have different absorption affinities with respect to adsorbing medium.What be suitable in principle in addition, is that all the components of admixture of gas has less loading when higher temperature on adsorbing medium.
The cycle of absorber process in the scope of the adsorption method of type of the present invention has two main stages.The removal of the reality of trace constituent to be separated is carried out during absorption phase.Its feature also is, the product gas mixture of discharging from absorber, discharge from this or these trace gas to be separated out---be referred to as product gas below---component substantially the same aspect the described principal component in the thick gas mixture that is delivered to this absorber the component of---below be referred to as thick gas---.
In the second main stage, (loading) adsorbing medium raises by the temperature by means of regeneration gas and flushing is regenerated, and promptly discharges from the trace constituent that has adsorbed.This second main stage is commonly called heating or heating period.
What be suitable on the principle is, regeneration-or the component of flushing gas can be same as or be different from the component of the thick gas that is delivered to this or these absorber.
Adsorption process or-method is called as T (emperature) S (wing) A (dsorption) method, wherein raises by temperature---and measure of other in case of necessity, as to support described loading adsorbing medium regeneration---and carry out the regeneration of the adsorbing medium of described loading.
Because adsorbate Neo-Confucianism when this adsorption process, one or more principal components of thick gas are very different between the end of the adsorbance on the adsorbing medium in the end of aforesaid heating period and absorption phase.In addition, this residual quantity is also owing to the different gas flow of each principal component in the void volume at absorber between the end of the end of heating period and absorption phase increases.
Therefore, owing to aforesaid reason, for one or more principal components that are contained in the thick gas, the TSA method is not only as remittance, and the source of being used as.Below, this difference is called as storage capacity.This storage capacity is in one-period---preferably when the beginning of heating period---to be released out and to be filled again again.During one-period, a kind of principal component can repeatedly be stored and be discharged, and is exactly this situation when certain components contents in the regeneration gas is higher than this kind components contents in the thick gas for example.
Because the TSA method (for example is used at H in continuous process
2Remove water and CO before/the CO ice chest
2) repeatedly introduced, so aforesaid source is converged characteristic and is interfered because handled like this, can be subjected on about the component aspect the principal component source of TSA to converge the fluctuation and will disturb gas separation process in ice chest subsequently thus unfriendly in short-term of characteristic restriction ground at it towards the gas stream of ice chest.
Explain the TSA method that belongs to prior art in detail by Fig. 1 and 2 below; At this, the TSA method realizes in two absorbers that are arranged in parallel.Following explaining also is applicable to the TSA method with three or more absorber that is arranged in parallel in a similar fashion on principle.
The notion of in Fig. 1, using " regeneration gas supply " and below the notion " regeneration gas body source " used should be understood that the source arbitrarily of regeneration gas.At this, the part that can use product gas and/or thick gas is as regeneration gas, and still, regeneration gas also can come from independently (" outside ") source of the gas.
In Fig. 1 and below the notion " regeneration gas extractor " used comprise each receiver arbitrarily for the employed gas of TSA of regenerating.It for example can be chimney, burner or other the device of burning gases.
Shown in figure 2, the cyclogram of example has following cycle (Takt) or stage; At this, represent the entrance side of absorber with label 1 with respect to the flow direction of thick gas, express oral-lateral with label 2:
A absorption: thick gas-flow direction 1 → 2 or A → B
Pa_A/B parallel running mode (optionally): two absorbers are carried thick gas simultaneously;
Flow direction 1 → 2 or A → B
The pressure of DA_A/B absorber pressure is adaptive
H heating: flow direction 1 → 2 or 2 → 1, preferred 2 → 1, but C → D always
K cools off (optionally): flow direction 1 → 2 or 2 → 1, and preferred 2 → 1,
But C → D always
The gas or the admixture of gas that use in stage H and K can be identical or different gas or admixture of gas.Therewith irrespectively, employed gas or admixture of gas all are called as regeneration gas below.
In order to simplify following explanation, suppose: these absorbers are not served as the holder of being worth mentioning during cycle DA_A/B.
If absorber lives through heating period H, it just uses the source of the principal component that acts on thick gas so.For this reason, the regeneration gas component on the D point (referring to Fig. 1) obviously is different from the regeneration gas component on the C point, because the regeneration gas on the D point additionally comprises the principal component that discharges and the trace constituent of thick gas.Do not wish the principal component content that increases of the thick gas in the regeneration gas especially for the follow-up process that is provided with in case of necessity, regeneration gas is transported to this follow-up process.
If regeneration gas is a kind of admixture of gas that is made of two or more compositions that have different absorption affinities on adsorbing medium, can cause other (secondary) source remittance characteristic so in principle.In cooling stage K, on the D point, draw the temporal fluctuation of the principal component of regeneration gas thus, because TSA during cooling uses the remittance (Senke) of the composition that acts on regeneration gas.
If regeneration gas comprises the composition of thick gas, compare with the heating period so, the part of the storage capacity that discharges during heating can be in cooling stage K lower temperature during by cooling compensate; This is to be worth expectation usually on principle.Yet thus in the enrichment of one or more compositions that yet cause thick gas on the D point and cause the fluctuation of regeneration gas component thus on the D point, this does not expect under the situation of a plurality of processes.If for example with the part of product gas with acting on the regeneration gas of heating and cooling and this regeneration gas being carried or be mixed to thick source of the gas again---for example have CO
2The steam reformer of washing causes the increasing and cause reducing of single principal component in the regeneration gas so under the situation of cooling under the situation of heating, thereby and cause TSA thus in thick gas and finally also cause in product gas.
Aforesaid main source is converged the final compensation of characteristic and is carried out during cycle DA_B, Pa_B and/or A.In that slightly the flow of gas principal component is more or less different with the flow on the B point consumingly on the A point, on the B point, cause the corresponding fluctuation of concentration of product gas thus thus.But for similar reason, this fluctuation of concentration is normally undesirable.
The filling of the storage capacity in the void volume does not have fuel factor ground and carries out.On the contrary, the filling of the storage capacity that has been adsorbed causes tangible fuel factor, is causing temperature to rise during the cycle Pa_A/B on the B point in short-term thus.
If regeneration gas has the temperature higher slightly than thick gas, absorber or adsorbing medium inadequately are cooled in cooling stage so, so, for this reason, in parallel running or in absorption phase, also cause the temperature of the product gas on the B point to raise between elementary period.
Summary of the invention
The objective of the invention is, propose method a kind of described type, that be used for removing from a kind of admixture of gas absorption ground with at least two kinds of other compositions (principal component) at least a composition that exists with the concentration less than 2% volume ratio (trace constituent), this method has been avoided above-mentioned shortcoming.Especially by means of method of the present invention concentration on B point and the D point and the temperature fluctuation on flowed fluctuation and the B point are minimized.
Method of the present invention has following steps:
A) the thick gas of input under adsorptive pressure is adsorbed on trace constituent on the adsorbing medium and the discharge product gas,
B) adsorbing medium that loads by means of regeneration gas body heating, this regeneration gas has than the high temperature of thick gas that is delivered to absorber between adsorption cycle, this regeneration gas is provided by a regeneration gas body source and it is transported to a regeneration gas body extractor after by absorber
C) make thick gas and/or product gas flow through adsorbing medium at least 30 minutes intermittently or continuously, wherein, this or these gas stream is transported to regeneration gas extractor and flow is 7% of the thick air-flow that inputs or outputs or product gas stream to the maximum during method step a) after flowing through adsorbing medium.
The interrupted quilt of absorber for example flow through by absorber boost and replacing of release produces.Thus, gas alternately flows into or flows out absorber.At this, temporal on average becoming a mandarin by the spent total gas flow that is used to boost divided by being used to boost and the merchant of total time of release calculates.Similarly, temporally on average go out stream and boost and the release time calculates divided by total by total release gas flow.Under the situation that the continuous quilt of absorber flows through, gas flows into simultaneously and flows out absorber.
Below, the aforesaid Continuous Flow of thick gas of the usefulness of adsorbing medium and/or product gas is crossed to be called as and is loaded compensation process (BE).BE expresses for the cycle: thick gas and/or product gas infeed in the absorber under a pressure that is between thick atmospheric pressure and the regeneration gas pressure, and slightly gas and/or product gas are transported to regeneration gas extractor D and are not delivered to product gas extractor B.At this, flow and/or temperature and time that the gas that infeeds at the C point flows change relatively like this, the feasible fluctuation that can keep permission on extractor D.
By using thick gas and/or product gas, not only aspect the void volume but also can both be aspect the adsorbance between the 0-100%, preferably in the compensation that realizes storage capacity more than 50%.In addition, the temperature of absorber preferably up to several degrees centigrade of ground by using enough gas flows and time to place on the level of adsorption cycle subsequently; When cooling step K only is set, can not accomplish this point.
Therefore, when parallel running stage subsequently of She Zhiing or absorption phase A, on the B point, can or only not cause the fluctuation of concentration in the product gas slightly where necessary.
Now, load that the heat of adsorption that occurs during the compensation process is sent by the direction towards regeneration gas extractor D and unlike the method that belongs to prior art during step or cycle Pa_A/B and/or A the direction towards product extractor B send.Unescapable temperature fluctuation always appears in (because heat is moved) on the D point, and this temperature fluctuation is undesirable on the B point and can avoids by method of the present invention.
Preferably use method of the present invention during less than adsorptive pressure at the pressure of regeneration gas.
The favourable configuration of other of the inventive method is characterised in that:
-after directly the absorption phase in an absorber finishes and directly the absorption phase in this absorber or another absorber infeeds thick gas to these two absorbers before beginning simultaneously,
-carry out absorber pressure and adsorptive pressure or regeneration gas pressure pressure adaptive---at this, this pressure adaptive can method step a) and c) and/or c) and a) carry out,
-at the adsorbing medium that begins to heat described loading (method step b)) before by means of regeneration gas body flushing absorber, the flow of this regeneration gas is less than the flow of the regeneration gas of the adsorbing medium that during heating is conducted through loading,
-in heating (method step b)) flow through adsorbing medium (method step c) afterwards and at thick gas and/or product gas) cool off adsorbing medium by leading of a regeneration gas body before, the temperature of this regeneration gas is lower than the temperature of the regeneration gas of the adsorbing medium that during heating is conducted through loading
-method step a) and c) and/or c) and carry out a release a) towards the regeneration gas extractor,
-method step a) and c) and/or c) and a) boost by thick gas and/or product gas, wherein, this thick gas and/or product gas preferably are directed the flow direction during the absorption phase,
-alternately repeat to boost-and the release stage, and
-regeneration gas has and thick gas phase component together.
Explain the possible configuration of the inventive method below in detail according to cyclogram shown in Figure 3.
The cycle mark representative of in Fig. 3, using:
A absorption: thick gas-flow direction 1 → 2 or A → B
Pa_A/B parallel running mode: two absorbers are carried thick gas simultaneously; Flow direction
1 → 2 or A → B
The pressure of DA_A/B absorber pressure is adaptive
H heating: the regeneration gas of Class1; Flow direction 1 → 2 or 2 → 1, excellent
Select 2 → 1, but C → D always
K cooling: Class1 or 2 regeneration gas; Flow direction 1 → 2 or 2 → 1,
Preferred 2 → 1, but C → D always
SP flushing: Class1 or 2 regeneration gas; Flow direction 1 → 2 or 2 → 1,
Preferred 2 → 1, but C → D always
K1 cools off first: Class1 or 2 regeneration gas; Flow direction 1 → 2
Or 2 → 1, preferred 2 → 1, but C → D always
K2 cools off second portion: Class1 or 2 regeneration gas; Flow direction 1 → 2
Or 2 → 1, preferred 2 → 1, but C → D always
BE loads compensation process: thick gas and/or product gas; Flow direction A → D
And/or B → D
Flushing cycle SP is mainly used in the slow and autotelic release of principal component of the storage of thick gas, not only from the intermediate volume of absorber but also from adsorbed amount.Thus, this absorber is used as the source now in this cycle.The flow and the temperature that flow into the regeneration gas in the absorber to be regenerated are optimised during this cycle, so that realize: the concentration on the D point-be within the scope of expectation with flowed fluctuation.Superfluous regeneration gas can flow through on absorber next door to be regenerated by means of a bypass line (this bypass line is as illustrated in fig. 1 like that).
Cooling cycle K1 is the first of the cooling stage of absorber to be regenerated.If absorber is cooled, it is always forcibly as converging so.For this reason, the flow of regeneration gas and enter temperature and regulated like this makes concentration on the D point-be within the scope of expectation with flowed fluctuation.During cooling cycle K1, also can superfluous regeneration gas be flow through on absorber next door to be regenerated by means of a bypass line.
During cooling cycle K2, the fluctuation of being worth mentioning of regeneration gas component on the D point, do not occur, so the regeneration gas scale of construction can maximize.If the component of regeneration gas component with thick gas aspect the content of one or more principal components is different, so during cooling storage capacity can be filled by halves.When the component of regeneration gas basic identical with the component of thick gas or product gas, but regeneration gas enter temperature when being higher than the temperature of thick gas, also this effect can appear.
Especially in this case it is significant being provided with and loading compensation process, because can compensate the storage capacity and/or the temperature of absorber thus.
According to one of the inventive method favourable configuration, as long as adsorptive pressure is higher than regeneration gas pressure, so method step a) and c) and/or just realize one c) and a) and boost by means of thick gas and/or product gas, wherein, this boost phase one or many ground, under repeated situation, preferably directly follow ground each other, alternately repeat with one or more release stages.
At this, thick gas and/or product gas preferably are directed the flow direction during the absorption phase.
Explain this configuration of method of the present invention below in detail according to the cyclogram shown in Fig. 4.
Except already used cycle mark in Fig. 3, the cyclogram shown in transit 4 also has two other cycles, that is:
D is by the release of absorber connecting portion D
R boosts by thick gas and/or product gas, preferably with adverse current (with respect to the flow direction of absorption)
If the pressure of regeneration gas is lower than the pressure of thick gas, can carry out boosting of absorber and release by the connecting portion that provides by thick gas and/or product gas so.
By preferably with boosting during R that the thick gas of adverse current and/or product gas carry out, cause storage capacity partly to be compensated.Under the situation of the suitable stress level---it needn't be reduced on the regeneration gas pressure---of the release of regeneration gas extractor D, thus avoided previous absorption principal component desorption and avoid it to flow away.In this method embodiment, gas is overflowed from the intermediate volume of absorber basically during release.This method causes thick gas and/or product gas to flow through adsorbing medium intermittently.
The aforesaid deformation program that boosts can arbitrary number of times ground repeat, up to the recharging almost completely of realizing storage capacity---amount of intermediate volume and absorption---.Among parallel running Pa_A/B subsequently or the absorption A subsequently, storage capacity only also needs to fill slightly where necessary; So in product gas (B), in fact do not cause fluctuation of concentration.
If in regeneration gas heaters, cause the chemical reaction of regeneration gas---especially under the situation of the high time of staying, advised another expansion of chart normal period so.Before cycle SP or H, wash this heater and the regeneration gas in the bypass is centered on the TSA guiding with regeneration gas.If this measure is introduced a distinctive cycle SE (flushing heater) realizing on the time sequencing after step DA so for this reason.If the flushing heater can be tolerated before step DA, during the parallel running mode, provide the flushing of heater so.In this case, this step is not shown in the cyclogram.
Claims (10)
1. be used for the method for removing at least a composition that exists with the concentration less than 2% volume ratio (trace constituent) at least on method that two absorbers that are arranged in parallel are realized absorption ground from a kind of admixture of gas with at least two kinds of other compositions (principal component) by means of a kind of, it has following method step:
A) when adsorptive pressure, import thick gas (A), be adsorbed on trace constituent on the adsorbing medium and discharge product gas (B),
B) adsorbing medium that loads by means of regeneration gas body heating, this regeneration gas has than the high temperature of thick gas that is delivered to absorber between adsorption cycle, this regeneration gas is provided by a regeneration gas body source (C) and it is transported to a regeneration gas body extractor (D) after by absorber
C) make thick gas and/or product gas flow through adsorbing medium at least 30 minutes intermittently or continuously, wherein, this or these gas stream is transported to described regeneration gas extractor (D) and flow is 7% of the thick air-flow that inputs or outputs or product gas stream to the maximum during method step a) after flowing through adsorbing medium.
2. by the described method of claim 1, it is characterized in that: after directly the absorption phase in an absorber finishes and directly the absorption phase in this absorber or another absorber infeeds thick gas to these two absorbers before beginning simultaneously.
3. by claim 1 or 2 described methods, it is characterized in that: the pressure that carries out absorber pressure and adsorptive pressure or regeneration gas pressure is adaptive.
4. by the described method of claim 3, it is characterized in that: method step a) and c) and/or c) and carry out between absorber pressure and adsorptive pressure, regeneration gas pressure or adsorptive pressure and the regeneration gas pressure each a) pressure of pressure is adaptive arbitrarily.
5. by one of claim 1-4 described method, it is characterized in that: at the adsorbing medium that begins to heat described loading (method step b)) before by means of regeneration gas body flushing absorber, the flow of this regeneration gas is less than the flow of the regeneration gas of the adsorbing medium that during heating is conducted through loading.
6. by one of claim 1-5 described method, it is characterized in that: in heating (method step b)) flow through adsorbing medium (method step c) afterwards and at thick gas and/or product gas) cool off adsorbing medium by leading of a regeneration gas body before, the temperature of this regeneration gas is lower than the temperature of the regeneration gas of the adsorbing medium that during heating is conducted through loading.
7. by the described method of one of claim 1-6, it is characterized in that: method step a) and c) or c) and carry out a release a) towards regeneration gas extractor (D).
8. by the described method of one of claim 1-7, it is characterized in that: method step a) and c) or c) and a) boost by thick gas and/or product gas, wherein, this gas preferably is directed the flow direction during the absorption phase.
9. by claim 7 and one of 8 described devices, it is characterized in that: alternately, repeat to boost to arbitrary number of times-and the release stage.
10. by one of claim 1-9 described device, it is characterized in that: described regeneration gas has and thick gas phase component together.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102005032025.2 | 2005-07-08 | ||
| DE102005032025A DE102005032025A1 (en) | 2005-07-08 | 2005-07-08 | Method for the adsorptive removal of trace components |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101218011A true CN101218011A (en) | 2008-07-09 |
Family
ID=36975253
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2006800249836A Pending CN101218011A (en) | 2005-07-08 | 2006-07-06 | Method for the removal of trace components by adsorption |
Country Status (8)
| Country | Link |
|---|---|
| EP (1) | EP1901828A1 (en) |
| JP (1) | JP2009500157A (en) |
| KR (1) | KR20080032051A (en) |
| CN (1) | CN101218011A (en) |
| DE (1) | DE102005032025A1 (en) |
| RU (1) | RU2008104175A (en) |
| TW (1) | TW200714344A (en) |
| WO (1) | WO2007006490A1 (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US9382399B2 (en) | 2011-05-13 | 2016-07-05 | Mas Innovation (Private) Limited | Foam composition and its uses thereof |
| WO2012156691A1 (en) | 2011-05-13 | 2012-11-22 | Mas Research And Innovation (Pvt) Ltd. | Method of manufacturing a fabric-laminated foam article |
| EP3216511A1 (en) * | 2016-03-08 | 2017-09-13 | Casale SA | A temperature-swing adsorption process |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE871886C (en) * | 1942-07-02 | 1953-03-26 | Linde Eismasch Ag | Adsorption process |
| US4479814A (en) * | 1980-07-07 | 1984-10-30 | Near Equilibrium Research Associates | Recirculation regeneration |
| US4784672A (en) * | 1987-10-08 | 1988-11-15 | Air Products And Chemicals, Inc. | Regeneration of adsorbents |
| FR2661841B1 (en) * | 1990-05-09 | 1992-07-17 | Air Liquide | AIR ADSORPTION CLEANING PROCESS AND APPARATUS FOR DISTILLE. |
| US5298054A (en) * | 1990-10-01 | 1994-03-29 | Fmc Corporation | Pressure and temperature swing adsorption system |
-
2005
- 2005-07-08 DE DE102005032025A patent/DE102005032025A1/en not_active Withdrawn
-
2006
- 2006-07-06 RU RU2008104175/15A patent/RU2008104175A/en unknown
- 2006-07-06 JP JP2008519866A patent/JP2009500157A/en active Pending
- 2006-07-06 KR KR1020077030903A patent/KR20080032051A/en not_active Application Discontinuation
- 2006-07-06 WO PCT/EP2006/006624 patent/WO2007006490A1/en active Application Filing
- 2006-07-06 TW TW095124575A patent/TW200714344A/en unknown
- 2006-07-06 CN CNA2006800249836A patent/CN101218011A/en active Pending
- 2006-07-06 EP EP06754683A patent/EP1901828A1/en not_active Ceased
Also Published As
| Publication number | Publication date |
|---|---|
| WO2007006490A1 (en) | 2007-01-18 |
| EP1901828A1 (en) | 2008-03-26 |
| RU2008104175A (en) | 2009-08-20 |
| JP2009500157A (en) | 2009-01-08 |
| TW200714344A (en) | 2007-04-16 |
| DE102005032025A1 (en) | 2007-01-18 |
| KR20080032051A (en) | 2008-04-14 |
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