CN206970202U - A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing - Google Patents
A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing Download PDFInfo
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- CN206970202U CN206970202U CN201720794541.5U CN201720794541U CN206970202U CN 206970202 U CN206970202 U CN 206970202U CN 201720794541 U CN201720794541 U CN 201720794541U CN 206970202 U CN206970202 U CN 206970202U
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- deoxidation
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- hot
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- 239000007789 gas Substances 0.000 title claims abstract description 54
- 239000001257 hydrogen Substances 0.000 title claims abstract description 52
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 52
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 49
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 21
- 239000012141 concentrate Substances 0.000 title claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000001301 oxygen Substances 0.000 claims abstract description 30
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 30
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 22
- 230000008676 import Effects 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 13
- 229910052763 palladium Inorganic materials 0.000 claims description 11
- 238000004891 communication Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 7
- 239000007788 liquid Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims 1
- 239000003034 coal gas Substances 0.000 abstract description 14
- 239000000571 coke Substances 0.000 description 14
- 238000000746 purification Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 230000008569 process Effects 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000006392 deoxygenation reaction Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Landscapes
- Separation Of Gases By Adsorption (AREA)
Abstract
A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing is the utility model is related to, it includes deoxidation tower, cooler and separator, it is characterized in that：Including a deoxidation tower and two heaters, described two heaters are respectively：Steam heater and deoxidation hot-air heater.The utility model effectively deviates from the oxygen in hydrogeneous coal gas, the oxygen content in coal gas is controlled in reasonable, safe range, thoroughly solve hydrogeneous coal gas super oxygen potential safety hazard by increasing deoxidation tower.
Description
Technical field
A kind of hydrogen manufacturing device for deoxidizing is the utility model is related to, particularly a kind of oxygen-containing raw coke oven gas PSA pressure swing adsorption hydrogen productions carry
Dense gas device for deoxidizing.Belong to field of chemical equipment.
Background technology
Semi-coke device uses the upright block furnace pyrolytic process technology of internal-combustion and-heating type, and device is by standby coal, charing, sieve fortune, coal
Gas purifies four parts composition.Gas purification workshop section uses m- direct-cooled technique, and raw coke oven gas is through at the beginning of cyclic ammonia water spraying cooling, transverse tube
Coal gas after cooler and electrical tar precipitator removing tar fog is pressurizeed with roots blower, and a part is melted down, and a part send drying bed, its
Remaining part is allocated as being sent to device for producing hydrogen extraction hydrogen for outer give gas.
Semi-coke raw coke oven gas main component：
The flow of raw coke oven gas PSA pressure swing adsorption hydrogen production devices is TSA+VPSA+PSA flows, and TSA is pretreatment process, main
Remove the impurity such as tar in coal gas, naphthalene, moisture；VPSA is hydrogen upgrading transformation vacuum suction flow, mainly by coal gas
Hydrogen content carrying to 45-50% by 25-29%；PSA is hydrogen purification pressure-variable adsorption flow, mainly by hydrogen purification extremely
99.99%, it is then sent to lower procedure.
Under normal circumstances, the oxygen content in semi-coke raw coke oven gas such as carbonizes 0.5% or so, but when production is fluctuated
When furnace pressure power, tolerance change, it can cause in raw coke oven gas that oxygen content is exceeded (reaching more than 1.0%), in VPSA pressure-variable adsorptions
During, due to the adsorption property that is not easy of oxygen, the oxygen content in concentrate gas can high 0.2% left side than the oxygen content in raw coke oven gas
The right side, the higher concentrate gas of this some oxygen content, after purification workshop section is entered, because enrichment phenomenon occurs for oxygen, cause hydrogen
In oxygen content can be higher, potential safety hazard be present.It is guarantee system fortune so how to remove the oxygen content in hydrogen upgrading gas
The only resource of row safety.
Utility model content
In order to solve the above problems, the purpose of this utility model PSA pressure swing adsorption hydrogen production concentrate gas device for deoxidizing, it can be incited somebody to action
Oxygen content in concentrate gas is controlled below 0.3%, ensures the control of purification system oxygen content in safe range, it is ensured that dress
Put safe for operation.
The technical solution of the utility model is：A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing, it includes concentrate gas
Deoxidation tower, two heaters, cooler and separator.It is characterized in that：Deoxidation tower is in the presence of palladium catalyst, oxygen and hydrogen
Reaction generation water, removes oxygen；Two described heaters are respectively：Steam heater and deoxidation hot-air heater；Hydrogen upgrading
Device is connected by the first valve and steam heater with deoxidation hot-air heater inlet and outlet respectively, the deoxidation hot-air heater disengaging
Mouth is divided into the first import, first outlet, the second import and second outlet；First valve and steam heater are all by the 4th valve
First inlet communication of door and deoxidation hot-air heater, the first valve and steam heater be all by the 8th valve respectively with deoxidation
The first outlet of hot-air heater and the inlet communication of deoxidation tower, the outlet of deoxidation tower pass through the 6th valve and deoxidation hot-air heater
Second inlet communication, the outlet of deoxidation tower also by the 7th valve respectively with the second outlet of deoxidation hot-air heater and cooler
Inlet communication, the 5th valve is provided with the second outlet of the deoxidation hot-air heater, the outlet of cooler connects with separator.
The entrance of the steam heater is provided with the second valve；Exit is provided with the 3rd valve.
The cooler is two, respectively deoxidation Gas Cooler A and deoxidation Gas Cooler B, the deoxidation Gas Cooler A
Imported and exported with deoxidation Gas Cooler B both ends in parallel respectively.
First valve, the 4th valve, the 5th valve, the 6th valve and the 7th valve are check-valves；Described 8th
Valve is stop valve.
Palladium catalyst is filled with the deoxidation tower.
The separator is gas-liquid separator.
Second valve and the 3rd valve are check-valves.
The advantages of the utility model：The utility model effectively removes hydrogeneous coal gas by increasing deoxidation tower after concentrate gas
In oxygen, oxygen content in coal gas is controlled in reasonable, safe range, thoroughly solve hydrogeneous coal gas super oxygen potential safety hazard.
Need to set steam heater before deoxidation tower is entered, ensure deoxidation tower palladium catalyst activationary temperature condition.And running
Cheng Zhong, because oxygen content fluctuation is larger in semi-coke raw coke oven gas, deoxidation heater can ensure, guarantor stable into deoxidation tower hydrogen temperature
Demonstrate,prove deoxidation effect.
The utility model is described in further details below by specific embodiment, but not as to of the present utility model
Limit.
Brief description of the drawings
Fig. 1 is structural representation of the present utility model；
In figure：1st, hydrogen upgrading device；2nd, steam heater；3rd, deoxidation hot-air heater；4th, deoxidation tower；5th, deoxidation air cooling
Device A；6th, deoxidation Gas Cooler B；7th, separator；8th, the first valve；9th, the second valve；10th, the 3rd valve；11st, the 4th valve；
12nd, the 8th valve；13rd, the 5th valve；14th, the 6th valve；15th, the 7th valve；16th, the first import；17th, first outlet；18th,
Two imports；19th, second outlet.
Embodiment
Embodiment 1
As shown in figure 1, a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing, it includes hydrogen upgrading device 1, cooling
Device, 7, deoxidation towers 4 of separator and two heaters, described two heaters are respectively：Steam heater 2 and deoxidation gas
Heater 3；Hydrogen upgrading device 1 is connected by the first valve 8 and steam heater 2 with the inlet and outlet of deoxidation hot-air heater 3 respectively,
The inlet and outlet of deoxidation hot-air heater 3 are divided into the first import 16, first outlet 7, the second import 18 and second outlet 19；First valve
Door 8 and steam heater 2 are all to be connected by the 4th valve 11 with the first import 16 of deoxidation hot-air heater 3, the He of the first valve 8
Steam heater 2 is connected respectively with the first outlet 17 of deoxidation hot-air heater 3 and the import of deoxidation tower 4 by the 8th valve 12
Logical, the outlet of deoxidation tower 4 is connected by the 6th valve 14 with the second import 18 of deoxidation hot-air heater 3, and the outlet of deoxidation tower 4 is also
Added respectively with the second outlet 19 of deoxidation hot-air heater 3 and the inlet communication of cooler, the deoxidation gas by the 7th valve 15
The 5th valve 13 is provided with the second outlet 19 of hot device 3, the outlet of cooler connects with separator 7.The deoxidation tower 4 is built-in
It is filled with palladium catalyst.
The pressure-variable adsorption of existing Adsorption Hydrogen device takes two-stage method to extract hydrogen, and first paragraph is hydrogen upgrading section, coal
Density of hydrogen is improved to 45-50% in gas.Second segment is hydrogen purification section, and hydrogen purity is carried to 99.99%.In actual motion mistake
Cheng Zhong, when the oxygen concentration in unstripped gas is more than 1.0%, oxygen content is more than 1.2%, during purification workshop section is along deflating in concentrate gas
Oxygen content is higher, potential safety hazard be present.
The utility model is controlled the oxygen content in hydrogen by exporting increase deoxidation tower in first paragraph hydrogen upgrading section
Below 0.3%, ensure safe for operation.Deoxidation, oxygen and hydrogen urging in palladium catalyst are carried out using palladium catalyst in deoxidation tower
The lower reaction production water of change effect, separates abjection in hydrogen after cooling.Needed to have due to the catalytic activity of palladium catalyst
Condition be under normal temperature carbon monoxide be less than 0.3% can activated catalyst activity, due to carbon monoxide 5-7% in enriching section hydrogen,
Activationary temperature must reach 80-120 DEG C, need to set steam heater before deoxidation tower is entered, and ensure that deoxidation tower palladium catalyst swashs
It is living.And in the process of running, due in semi-coke raw coke oven gas oxygen content fluctuation it is larger, deoxidation heater can ensure into deoxidation tower
Hydrogen temperature is stable, ensures deoxidation effect.
Embodiment 2
As shown in figure 1, a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing, it includes hydrogen upgrading device 1, cooling
Device, 7, deoxidation towers 4 of separator and two heaters, described two heaters are respectively：Steam heater 2 and deoxidation gas
Heater 3；Hydrogen upgrading device 1 is connected by the first valve 8 and steam heater 2 with the inlet and outlet of deoxidation hot-air heater 3 respectively,
The inlet and outlet of deoxidation hot-air heater 3 are divided into the first import 16, first outlet 7, the second import 18 and second outlet 19；First valve
Door 8 and steam heater 2 are all to be connected by the 4th valve 11 with the first import 16 of deoxidation hot-air heater 3, the He of the first valve 8
Steam heater 2 is connected respectively with the first outlet 17 of deoxidation hot-air heater 3 and the import of deoxidation tower 4 by the 8th valve 12
Logical, the outlet of deoxidation tower 4 is connected by the 6th valve 14 with the second import 18 of deoxidation hot-air heater 3, and the outlet of deoxidation tower 4 is also
Added respectively with the second outlet 19 of deoxidation hot-air heater 3 and the inlet communication of cooler, the deoxidation gas by the 7th valve 15
The 5th valve 13 is provided with the second outlet 19 of hot device 3, the outlet of cooler connects with separator 7.The steam heater 2
Entrance be provided with the second valve 9；Exit is provided with the 3rd valve 10.
Palladium catalyst is filled with the deoxidation tower 4.The separator 7 is gas-liquid separator.
The cooler is two, respectively deoxidation Gas Cooler A5 and deoxidation Gas Cooler B6,
The deoxidation Gas Cooler A5 and deoxidation Gas Cooler B6 both ends inlet and outlet are in parallel respectively.
The course of work is as follows：First valve 8, the 8th valve 12 and the 7th valve 15 are closed, open the second valve 9, the
Three valves 10, the 4th valve 11, the 5th valve 13 and the 6th valve 14；The hydrogeneous coal gas 30-40 come out from hydrogen upgrading device 1
DEG C, 80-120 DEG C is heated to by steam heater 2, is changed in deoxidation hot-air heater 3 with the high-temperature gas after deoxygenation
Reach 150-180 DEG C after heat, into deoxidation tower 4, in the presence of palladium catalyst, hydrogen and oxygen reaction generation in coal gas
Water, the Control for Oxygen Content in coal gas is below 0.3% safety index.250-320 DEG C of gas temperature after deoxidation, into deoxidation
After hot-air heater 3 reclaims heat of reaction, 40-60 DEG C is cooled to through water recirculator, after delivering to gas-liquid separator separates water outlet,
Into next workshop section's hydrogen purification section.Deoxidation Deethanizer design maximum temperature≤400 DEG C, dehydrogenation catalyst reaction initial temperature 120-
160℃。
When need not use the deoxidation tower to carry out deoxidation, directly the second valve 9 of closing, the 3rd valve 10, the 8th valve 12, the
Six valves 14 and the 7th valve 15, the first valve 8, the 4th valve 11 and the 5th valve 13 are opened, is come out from hydrogen upgrading device 1
Hydrogeneous coal gas be directly over cooler cooling after, after delivering to gas-liquid separator separates water outlet, into next workshop section's hydrogen purification
Section.
Embodiment 3
On the basis of embodiment 2, first valve 8, the 4th valve 11, the 5th valve 13, the 6th valve 14 and
Seven valves 15 are check-valves；8th valve 12 is stop valve.The valve 10 of second valve 9 and the 3rd is non-return
Valve.
The part and the well-known components and common structure of the structure category industry or conventional hand that the present embodiment does not describe in detail
Section, is not described one by one here.
Claims (7)
1. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing, it includes hydrogen upgrading device (1), cooler and separator
(7), it is characterized in that：Also include a deoxidation tower (4) and two heaters, described two heaters are respectively：Steam heats
Device (2) and deoxidation hot-air heater (3)；Hydrogen upgrading device (1) is respectively by the first valve (8) and steam heater (2) with taking off
Oxygen heater (3) inlet and outlet connection, deoxidation hot-air heater (3) inlet and outlet are divided into the first import (16), first outlet
(17), the second import (18) and second outlet (19)；First valve (8) and steam heater (2) are all by the 4th valve
(11) connected with the first import (16) of deoxidation hot-air heater (3), the first valve (8) and steam heater (2) are all by
Eight valves (12) respectively with the first outlet (17) of deoxidation hot-air heater (3) and the inlet communication of deoxidation tower (4), deoxidation tower (4)
Outlet connected by the 6th valve (14) with the second import (18) of deoxidation hot-air heater (3), the outlet of deoxidation tower (4) is also logical
Cross the 7th valve (15) respectively with the second outlet (19) of deoxidation hot-air heater (3) and the inlet communication of cooler, the deoxidation
Second outlet (19) place of hot-air heater (3) is provided with the 5th valve (13), and the outlet of cooler connects with separator (7).
2. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 1, it is characterized in that：The steam
The entrance of heater (2) is provided with the second valve (9)；Exit is provided with the 3rd valve (10).
3. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 1, it is characterized in that：The cooling
Device is two, respectively deoxidation Gas Cooler A (5) and deoxidation Gas Cooler B (6), the deoxidation Gas Cooler A (5) and deoxidation
Gas Cooler B (6) both ends inlet and outlet are in parallel respectively.
4. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 1, it is characterized in that：Described first
Valve (8), the 4th valve (11), the 5th valve (13), the 6th valve (14) and the 7th valve (15) are check-valves；Described
Eight valves (12) are stop valve.
5. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 1, it is characterized in that：The deoxidation
Palladium catalyst is filled with tower (4).
6. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 1, it is characterized in that：The separation
Device (7) is gas-liquid separator.
7. a kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing according to claim 2, it is characterized in that：Described second
Valve (9) and the 3rd valve (10) are check-valves.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720794541.5U CN206970202U (en) | 2017-07-03 | 2017-07-03 | A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720794541.5U CN206970202U (en) | 2017-07-03 | 2017-07-03 | A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN206970202U true CN206970202U (en) | 2018-02-06 |
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ID=61406963
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| CN201720794541.5U Active CN206970202U (en) | 2017-07-03 | 2017-07-03 | A kind of PSA pressure swing adsorption hydrogen productions concentrate gas device for deoxidizing |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112844492A (en) * | 2021-01-04 | 2021-05-28 | 新疆宣力环保能源有限公司 | Vulcanization method and system of shift reaction catalyst for hydrogen production from raw gas and shift hydrogen production process |
-
2017
- 2017-07-03 CN CN201720794541.5U patent/CN206970202U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112844492A (en) * | 2021-01-04 | 2021-05-28 | 新疆宣力环保能源有限公司 | Vulcanization method and system of shift reaction catalyst for hydrogen production from raw gas and shift hydrogen production process |
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| GR01 | Patent grant | ||
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Effective date of registration: 20241010 Granted publication date: 20180206 |