CN101850949A - Method with high purity and high recovery rate for purifying hydrogen gas in coke oven gas - Google Patents
Method with high purity and high recovery rate for purifying hydrogen gas in coke oven gas Download PDFInfo
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- CN101850949A CN101850949A CN 201010203034 CN201010203034A CN101850949A CN 101850949 A CN101850949 A CN 101850949A CN 201010203034 CN201010203034 CN 201010203034 CN 201010203034 A CN201010203034 A CN 201010203034A CN 101850949 A CN101850949 A CN 101850949A
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- 239000007789 gas Substances 0.000 title claims abstract description 107
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 238000011084 recovery Methods 0.000 title claims abstract description 27
- 238000000034 method Methods 0.000 title claims abstract description 22
- 239000000571 coke Substances 0.000 title abstract description 7
- 239000001257 hydrogen Substances 0.000 claims abstract description 94
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 94
- 239000012528 membrane Substances 0.000 claims abstract description 25
- 239000012535 impurity Substances 0.000 claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 14
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims abstract description 11
- 238000003795 desorption Methods 0.000 claims abstract description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000001301 oxygen Substances 0.000 claims abstract description 8
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 8
- 230000009466 transformation Effects 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 18
- 238000000746 purification Methods 0.000 claims description 7
- 238000002336 sorption--desorption measurement Methods 0.000 claims description 7
- 238000005202 decontamination Methods 0.000 claims description 5
- 230000003588 decontaminative effect Effects 0.000 claims description 5
- 238000001035 drying Methods 0.000 claims description 5
- 230000008595 infiltration Effects 0.000 claims description 5
- 238000001764 infiltration Methods 0.000 claims description 5
- 239000002594 sorbent Substances 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 239000003463 adsorbent Substances 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 2
- 229910052802 copper Inorganic materials 0.000 claims description 2
- 238000007791 dehumidification Methods 0.000 claims description 2
- 239000000835 fiber Substances 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims description 2
- 229910052748 manganese Inorganic materials 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 229910052759 nickel Inorganic materials 0.000 claims description 2
- 239000008041 oiling agent Substances 0.000 claims description 2
- 229910052763 palladium Inorganic materials 0.000 claims description 2
- 229910052697 platinum Inorganic materials 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 238000000926 separation method Methods 0.000 abstract description 19
- 230000008901 benefit Effects 0.000 abstract description 3
- 230000008859 change Effects 0.000 abstract description 3
- 230000000694 effects Effects 0.000 abstract description 2
- 150000001491 aromatic compounds Chemical class 0.000 abstract 1
- 230000007547 defect Effects 0.000 abstract 1
- 239000002994 raw material Substances 0.000 abstract 1
- 239000002641 tar oil Substances 0.000 abstract 1
- 238000010521 absorption reaction Methods 0.000 description 47
- 230000008569 process Effects 0.000 description 11
- 230000008878 coupling Effects 0.000 description 5
- 238000010168 coupling process Methods 0.000 description 5
- 238000005859 coupling reaction Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 5
- 230000000274 adsorptive effect Effects 0.000 description 3
- 238000006356 dehydrogenation reaction Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Separation Of Gases By Adsorption (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention relates to a method with high purity and high recovery rate for purifying hydrogen gas in coke oven gas, which belongs to the technical field of petrochemical industry. The method is characterized in that coke oven gas enters a pressure swing adsorption device to obtain hydrogen gas with the purity greater than 99.9v% after the impurities of naphthalinum, tar oil, NH3, H2S, other aromatic compounds and the like in the coke oven gas are removed by temperature swing adsorption, and high-purity hydrogen with the purity greater than 99.999v%, the oxygen content smaller than 3ppm and the dew point lower than -70 DEG C is obtained after the hydrogen gas is further deoxidated and dried; the purity of the hydrogen gas in pressure swing adsorption and desorption gas is greater than 20v%, the hydrogen gas enters a membrane separation device after the hydrogen gas is compressed and cooled, the obtained osmosis gas with the purity of 55 to 65v% of the hydrogen gas is returned to a compressor of the coke oven gas, and the hydrogen gas in the osmosis gas is further recovered; and the residual osmosis gas is discharged out of the battery limit of the device. The invention has the effects and advantages of making up the defects of low recovery rate of the pressure swing adsorption device and larger fluctuation generated along with the change of the purity of the raw material of the hydrogen gas and realizing that the hydrogen gas in the coke oven gas is purified with high purity and high recovery rate.
Description
Technical field
The invention belongs to the petrochemical technology field, relate to a kind of from coke-oven gas the separation method of high purity, high-recovery purifying hydrogen of hydrogen, specially refer to the method for hydrogen in the coke-oven gas that produces in the processes such as purification coking that adopt alternating temperature absorption, transformation absorption and membrane sepn coupled method high purity, high-recovery.
Background technology
Coke-oven gas is the gas that steel mill and coke factory produce in process of coking, the general 270～350Nm that produces of one ton of Jiao of every refining
3Coke-oven gas.This part gas composition complexity based on hydrogen and methane, contains a spot of carbon monoxide, carbonic acid gas, oxygen, nitrogen and hydro carbons simultaneously, also has micro-naphthalene and tar etc. in addition.Its classical group becomes to see Table 1.
Table 1 coke-oven gas the typical case form
Hydrogen is a kind of important chemical material and industrial protection gas, has a wide range of applications in synthetic ammonia, oil refining, electronics and metallurgical industry.Because the increasingly stringent that good combustionproperty that hydrogen had and environmental regulation require, the future market has the potential great demand to hydrogen.
Contain a large amount of hydrogen (about 55v%) in the coke-oven gas,, can cause the waste of hydrogen resource if directly burn as industry or domestic fuel.
Coke-oven gas Hydrogen Separation and purification techniques mainly contain separation by deep refrigeration, pressure swing adsorption process and membrane separation process.The hydrogen content that separation by deep refrigeration finally obtains is 83v%～88v%, and purity is not high, and equipment used is complicated and need operate under condition of high voltage, and it is big to produce investment.Transformation absorption is one of gas separation with fastest developing speed in recent decades, can produce highly purified hydrogen, but the rate of recovery is not high and change generation than great fluctuation process with the unstripped gas hydrogen purity; Membrane separation process has investment advantage little, simple to operate, but the purity of recover hydrogen is not high.
Owing to contain impurity such as heavy hydrocarbon and tar in the coke-oven gas, need earlier by just entering the psa unit purifying hydrogen of hydrogen after the alternating temperature absorption pre-treatment; Traditional coke-oven gas transformation absorption can obtain the hydrogen of purity greater than 99.9v%; Refining by deoxidation and drying process, can be met the High Purity Hydrogen (purity 99.999v%, oxygen level are lower than-70 ℃ less than 3ppm and dew point) that the cold-reduced sheet reducing gas requires.But the hydrogen recovery rate of coke-oven gas transformation absorption has only about 80% usually, still contains the hydrogen greater than 20v% in the stripping gas of generation.How to utilize the hydrogen in this part stripping gas still not have relevant report at present.
Summary of the invention
The method that the purpose of this invention is to provide hydrogen in a kind of high purity, the high-recovery purification coke-oven gas, this method adopt alternating temperature absorption, transformation absorption and membrane sepn coupled method.Coke-oven gas is in alternating temperature adsorbing and removing coke-oven gas behind the impurity, utilize pressure-swing absorption apparatus to obtain the higher hydrogen of purity, enter after simultaneously the stripping gas of pressure-swing absorption apparatus being boosted and turn back to the pressure-swing absorption apparatus inlet after membrane separation unit improves hydrogen purity, further reclaim hydrogen wherein; When guaranteeing hydrogen purity, improve hydrogen recovery rate.
The technical solution used in the present invention is: coke-oven gas at first enters into surge tank, enters the alternating temperature absorbing unit after entering then that first compressor boosts and be cooled to 40～60 ℃ in first water cooler and removes naphthalene, tar, NH
3, H
2Impurity such as S and other aromatics; Gas after the removal of impurities further improves pressure through second, third compressor, enters psa unit be cooled to 40～60 ℃ in second, third water cooler after, by selecting adsorbing and removing overwhelming majority impurity, obtains the hydrogen of purity greater than 99.9v%.
After the hydrogen of pressure varying adsorption of purified was sent into the further processing of deoxidation moisture eliminator, the High Purity Hydrogen purity that obtains was greater than 99.999v%, and oxygen level is less than 3ppm, and dew point is lower than-70 ℃, satisfies the requirement of cold-reduced sheet reducing gas; Transformation adsorption-desorption gas boosts and enters the gas film separating unit after laggard inlet/outlet water cooler is cooled to 40～75 ℃ from entering the stripping gas compressor, and hydrogen purity is that the infiltration gas of 55～65v% turns back to the surge tank before the coke-oven gas compressor; Ooze residual air discharger battery limit (BL).
In the described alternating temperature absorbing unit, the sorbent material of filling has de-oiling agent, gac and activated alumina.
Described psa unit is made up of oil removing tower, adsorption tower, suitable slowing down towards filling and hydrogen gas buffer; Its pattern is normal pressure desorb PSA device or vacuum desorption PSA device; Filling special-purpose activated charcoal and adsorbent of molecular sieve in the adsorption tower.
Described deoxidation and dry decontamination unit, the used catalyzer of deoxidation tower comprises the catalyzer of Pd, Pt, Cu, Mn, Ni series; The TSA dehumidification system that drying installation is made up of predrying tower, drying tower, branch flow container and interchanger.
Described gas delivery film unit is selected the vitreous state polymeric membrane assembly that hydrogen is had highly selective and perviousness for use, and its pattern comprises hollow-fibre membrane, spiral wound or plate and frame structure.
Effect of the present invention and benefit are: in the method for hydrogen, adopt alternating temperature absorption, transformation absorption and membrane sepn coupling in this purification coke-oven gas; Coke-oven gas is in alternating temperature adsorbing and removing coke-oven gas behind the impurity, utilize pressure-swing absorption apparatus to obtain the higher hydrogen of purity, adopt membrane separation unit that the hydrogen purity in the transformation adsorption-desorption gas is brought up to the scope close with coke-oven gas simultaneously, be re-used as the unstripped gas of pressure-swing absorption apparatus, further reclaim hydrogen wherein, it is high and change the defective that takes place than great fluctuation process with the unstripped gas hydrogen purity to have remedied the pressure-swing absorption apparatus rate of recovery; Realized hydrogen in high purity, the high-recovery purification coke-oven gas.For hydrogen content is the coke-oven gas of 55～60v%, though pressure-swing absorption apparatus can obtain the hydrogen of purity greater than 99.9v%, hydrogen recovery rate has only about 80%, and takes place when the unstripped gas hydrogen purity changes than great fluctuation process; After increasing membrane separation unit, can will further reclaim wherein hydrogen as the pressure-swing absorption apparatus unstripped gas behind the hydrogen upgrading in the stripping gas, under the prerequisite that guarantees hydrogen purity,, the unstripped gas hydrogen purity also the rate of recovery of hydrogen can be remained on about 95% even changing.
Description of drawings
Fig. 1 is that hydrogen process flow sheet in the coke-oven gas is reclaimed in alternating temperature absorption, transformation absorption.
Fig. 2 is that alternating temperature absorption, transformation absorption are reclaimed hydrogen process flow sheet in the coke-oven gas with the membrane sepn coupling.
Among the figure: 1 surge tank; 2 first compressors; 3 first water coolers; 4 alternating temperature absorbing units; 5 second, third compressors; 6 second, third water coolers; 7 psa units; 8 deoxidation moisture eliminators; 9 stripping gas compressors; 10 outlet water coolers; 11 gas delivery film units; The A coke-oven gas; The B High Purity Hydrogen; The C gas separation membrane oozes residual air; D transformation adsorption-desorption gas.
Embodiment
Be described in detail specific embodiments of the invention below in conjunction with technical scheme and accompanying drawing.
Embodiment 1
This example is that hydrogen content is the coke-oven gas of 59.56v%, adopts alternating temperature absorption, transformation absorption and the technical process of membrane sepn coupling recover hydrogen.
As shown in Figure 2, coke-oven gas enters surge tank 1 under 0.1MPa, after first compressor 2 is brought up to pressure 0.32MPa and reduced the temperature to 40 ℃ by first water cooler 3, enters into alternating temperature absorbing unit 4 and removes naphthalene, tar, NH
3, H
2S and other aromatics; Gas is further brought up to 1.8MPa with pressure and after second, third water cooler 6 is cooled to 40 ℃ through second, third compressor 5 after the removal of impurities, enter psa unit 7, the condition of selecting absorption at sorbent material is the most impurity of property except that dehydrogenation next time, the hydrogen of acquisition purity＞99.9v%.
Transformation adsorption-desorption gas enters gas film separating unit 11 after discharging at the bottom of the absorption Tata and pressure being brought up to 2.0MPa and be cooled to 60 ℃ by outlet water cooler 10 through stripping gas compressor 9; Hydrogen purity is that the surge tank 1 that the infiltration gas of 69.74v% turns back to inlet is mixed into device with coke-oven gas, oozes residual air discharger battery limit (BL).
Alternating temperature absorption adsorptive pressure is 0.32MPa in the present embodiment, adsorption temp: normal temperature; Desorption pressures: 0.12MPa, desorption temperature: 160～40 ℃.
Three pressure equalizings of five towers are adopted in transformation absorption, and hydrogen recovery rate is 83%.
The hydrogen recovery rate of gas separation membrane is 95.28%.
In this case study on implementation, the total yield of hydrogen is 96.5%, and the hydrogen purity of pressure-swing absorption apparatus is greater than 99.9v%; Obtain purity 99.999v%, oxygen level less than the High Purity Hydrogen that 3ppm and dew point are lower than-70 ℃ through deoxidation and dry decontamination technology, satisfy the requirement of cold-reduced sheet reducing gas.
This example is that hydrogen content is the coke-oven gas of 55.46v%, adopts alternating temperature absorption, transformation absorption and the technical process of membrane sepn coupling recover hydrogen.
Shown in Figure 2, coke-oven gas enters surge tank 1 under 0.1MPa, after first compressor 2 is brought up to pressure 0.32MPa and reduced the temperature to 40 ℃ by first water cooler 3, enters into alternating temperature absorbing unit 4 and removes naphthalene, tar, NH
3, H
2S and other aromatics; After gas is further brought up to pressure in 1.8MPa and second, third water cooler 6 and is cooled to 40 ℃ through second, third compressor 5 after the removal of impurities, enter psa unit 7, the condition of selecting absorption at sorbent material is the most impurity of property except that dehydrogenation next time, the hydrogen of acquisition purity＞99.9v%.
Transformation adsorption-desorption gas enters gas film separating unit 11 after discharging at the bottom of the absorption Tata and pressure being brought up to 2.0MPa and be cooled to 60 ℃ by outlet water cooler 10 through stripping gas compressor 9; Hydrogen purity is that the surge tank 1 that the infiltration gas of 76.43v% turns back to inlet is mixed into device with coke-oven gas, oozes residual air discharger battery limit (BL).
Alternating temperature absorption adsorptive pressure is 0.32MPa in the present embodiment, adsorption temp: normal temperature; Desorption pressures: 0.12MPa, desorption temperature: 160～40 ℃.
Three pressure equalizings of five towers are adopted in transformation absorption, because hydrogen purity reduces in the unstripped gas, the hydrogen recovery rate of pressure-swing absorption apparatus is reduced to 78%.
The hydrogen recovery rate of gas separation membrane is 96.2%.
In this case study on implementation, the total yield of hydrogen is 95.8%, and the hydrogen purity of pressure-swing absorption apparatus is greater than 99.9v%; Obtain purity 99.999v%, oxygen level less than the High Purity Hydrogen that 3ppm and dew point are lower than-70 ℃ through deoxidation and dry decontamination technology, satisfy the requirement of cold-reduced sheet reducing gas.
Embodiment 3
This example is that hydrogen content is the coke-oven gas of 59.56v%, adopts alternating temperature absorption, transformation absorption and the technical process of membrane sepn coupling recover hydrogen.
Shown in Figure 2, coke-oven gas enters surge tank 1 under 0.1MPa, after first compressor 2 is brought up to pressure 0.32MPa and reduced the temperature to 40 ℃ by first water cooler 3, enters into alternating temperature absorbing unit 4 and removes naphthalene, tar, NH
3, H
2S and other aromatics; Gas is further brought up to 1.8MPa with pressure and after second, third water cooler 6 is cooled to 40 ℃ through second, third compressor 5 after the removal of impurities, enter psa unit 7, the condition of selecting absorption at sorbent material is the most impurity of property except that dehydrogenation next time, the hydrogen of acquisition purity＞99.9v%.
Transformation adsorption-desorption gas enters gas film separating unit 11 after discharging at the bottom of the absorption Tata and pressure being brought up to 1.0MPa and be cooled to 60 ℃ by outlet water cooler 10 through stripping gas compressor 9; Hydrogen purity is that the surge tank 1 that the infiltration gas of 67.27v% turns back to inlet is mixed into device with coke-oven gas, oozes residual air discharger battery limit (BL).
Alternating temperature absorption adsorptive pressure is 0.32MPa in the present embodiment, adsorption temp: normal temperature; Desorption pressures: 0.12MPa, desorption temperature: 160～40 ℃.
Three pressure equalizings of five towers are adopted in transformation absorption, and hydrogen recovery rate is 83%.
Gas separation membrane is owing to the reduction of working pressure, and its hydrogen recovery rate is reduced to 85.31%.
In this case study on implementation, the total yield of hydrogen is 94.5%, and the hydrogen purity of pressure-swing absorption apparatus is greater than 99.9v%; Obtain purity 99.999v%, oxygen level less than the High Purity Hydrogen that 3ppm and dew point are lower than-70 ℃ through deoxidation and dry decontamination technology, satisfy the requirement of cold-reduced sheet reducing gas.
Among above-mentioned three embodiment, when hydrogen purity in the coke-oven gas reduced, the rate of recovery can reduce when pressure-swing absorption apparatus will guarantee the hydrogen purity of the 99.9v% that reaches; But behind the increase membrane separation unit,, still can guarantee to keep the rate of recovery of hydrogen to be not less than 95% under the constant situation of pressure-swing absorption apparatus hydrogen product purity even the unstripped gas hydrogen purity descends; Therefore increase the rate of recovery that membrane separation unit has not only improved hydrogen, also improved the stability of pressure-swing absorption apparatus operation simultaneously, enlarged operating restraint.
Among above-mentioned three embodiment, when the gas separation membrane working pressure raise, the rate of recovery of hydrogen also can increase; Higher relatively gas separation membrane working pressure more helps improving the rate of recovery of hydrogen.
Claims (1)
1. the method for hydrogen in a high purity, the high-recovery purification coke-oven gas is characterized in that:
Coke-oven gas at first enters into surge tank (1), enters alternating temperature absorbing unit (4) after entering then that first compressor (2) boosts and be cooled to 40～60 ℃ in first water cooler (3) and removes naphthalene, tar, NH
3, H
2Impurity such as S and other aromatics; Gas after the removal of impurities further improves pressure through second, third compressor (5), enter psa unit (7) after in second, third water cooler (6), being cooled to 40～60 ℃, by selecting adsorbing and removing overwhelming majority impurity, obtain the hydrogen of purity greater than 99.9v%;
After the hydrogen of pressure varying adsorption of purified was sent into the further processing of deoxidation moisture eliminator (8), the High Purity Hydrogen purity that obtains was greater than 99.999v%, and oxygen level is less than 3ppm, and dew point is lower than-70 ℃, satisfies the requirement of cold-reduced sheet reducing gas; Transformation adsorption-desorption gas boosts and enters gas film separating unit (11) after laggard inlet/outlet water cooler (10) is cooled to 40～75 ℃ from entering stripping gas compressor (9), and hydrogen purity is that the infiltration gas of 55～65v% turns back to the surge tank (1) before the coke-oven gas compressor; Ooze residual air discharger battery limit (BL);
In the described alternating temperature absorbing unit, the sorbent material of filling has de-oiling agent, gac and activated alumina;
Described psa unit is made up of oil removing tower, adsorption tower, suitable slowing down towards filling and hydrogen gas buffer; Its pattern is normal pressure desorb PSA device or vacuum desorption PSA device; Filling special-purpose activated charcoal and adsorbent of molecular sieve in the adsorption tower;
Described deoxidation and dry decontamination unit, the used catalyzer of deoxidation tower comprises the catalyzer of Pd, Pt, Cu, Mn, Ni series; The TSA dehumidification system that drying installation is made up of predrying tower, drying tower, branch flow container and interchanger;
Described gas delivery film unit is selected the vitreous state polymeric membrane assembly that hydrogen is had highly selective and perviousness for use, and its pattern comprises hollow-fibre membrane, spiral wound or plate and frame structure.
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