CN115253595A - System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application - Google Patents
System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application Download PDFInfo
- Publication number
- CN115253595A CN115253595A CN202210982399.2A CN202210982399A CN115253595A CN 115253595 A CN115253595 A CN 115253595A CN 202210982399 A CN202210982399 A CN 202210982399A CN 115253595 A CN115253595 A CN 115253595A
- Authority
- CN
- China
- Prior art keywords
- swing adsorption
- pressure swing
- hydrogen
- gas
- stage pressure
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000001179 sorption measurement Methods 0.000 title claims abstract description 95
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 85
- 239000001257 hydrogen Substances 0.000 title claims abstract description 84
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 238000000034 method Methods 0.000 title claims abstract description 48
- 239000007789 gas Substances 0.000 claims abstract description 134
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 239000000047 product Substances 0.000 claims description 35
- 238000000746 purification Methods 0.000 claims description 25
- 239000012467 final product Substances 0.000 claims description 10
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 3
- 150000002431 hydrogen Chemical class 0.000 abstract description 11
- 239000012535 impurity Substances 0.000 abstract description 10
- 238000004364 calculation method Methods 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract description 2
- 239000003463 adsorbent Substances 0.000 description 20
- 238000011084 recovery Methods 0.000 description 8
- 101150008822 rpsA gene Proteins 0.000 description 7
- 239000000571 coke Substances 0.000 description 5
- 238000010926 purge Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 4
- 150000002430 hydrocarbons Chemical class 0.000 description 4
- 239000004215 Carbon black (E152) Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000007689 inspection Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000010962 carbon steel Substances 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000013433 optimization analysis Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000012954 risk control Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012795 verification Methods 0.000 description 1
Images
Classifications
-
- 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
- B01D53/047—Pressure swing adsorption
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
Abstract
The invention relates to a system for purifying hydrogen by two-stage pressure swing adsorption, a method for purifying hydrogen and application thereof, wherein the system comprises a compressor, a first-stage pressure swing adsorption device and a second-stage pressure swing adsorption device which are sequentially connected; when the system for purifying hydrogen by two-stage pressure swing adsorption provided by the invention is used for purifying hydrogen, the high-impurity and low-hydrogen-containing raw material gas is finally treated by the combination of two-stage pressure swing adsorption devices, iterative calculation is carried out, the yield of hydrogen can be more than or equal to 80% while the requirement of high-purity product hydrogen is met, compared with the condition that one set of pressure swing adsorption device is directly used, the yield is improved by at least 10%, and the system is suitable for industrial production and application.
Description
Technical Field
The invention relates to the technical field, in particular to a system for purifying hydrogen by two-stage pressure swing adsorption, a method for purifying hydrogen and application.
Background
The hydrogen energy is a green and efficient secondary energy, and several factors such as reproducibility, efficiency and environmental friendliness are the most remarkable advantages of the hydrogen energy. The requirements of industries such as metallurgy, aerospace, electronics, glass, fine chemical engineering, energy and the like on the hydrogen energy and the purity are higher and higher.
Compared with the existing several process routes for purifying hydrogen at the present stage, when the product gas meets the requirements of pure hydrogen, high-purity hydrogen, even ultra-pure hydrogen and hydrogen for the electronic industry, only a pressure swing adsorption device is used, and the advantages of strong product purity adjustability and capability of simultaneously removing various impurity components by one-time separation are obtained in a plurality of methods, so that the method becomes a preferred method for purifying high-purity hydrogen. In addition, when the method is used for purifying hydrogen, the pressure loss of the product gas is not large, and the energy consumption is saved for the subsequent working section. However, the biggest problem is that the hydrogen yield of the product gas is generally not high, especially when the quality of the raw material gas is poor and the content of hydrogen is not high, the final hydrogen yield can only reach as low as 60% or even can not meet the product requirement by using a single pressure swing adsorption device.
CN113200518A discloses a method for recovering and purifying hydrogen from semi-coke tail gas, the semi-coke tail gas enters a two-section pressure swing adsorption hydrogen purification device under lower pressure after the procedures of purification, first compression, desulfurization and the like, the first section pressure swing adsorption device is regenerated by using a flushing method, and most of CO in the semi-coke tail gas is regenerated 2 、C 2+ Removing, while also removing part of N 2 、CO、CH 4 Waiting for impurity gas to obtain H 2 And N 2 The purified gas as main component is compressed for the second time, boosted and fed into the second stage pressure-variable adsorption equipment under the higher pressure to obtain H 2 The purity of the product hydrogen is more than or equal to 99 percent. The method recovers and purifies the hydrogen in the semi-coke tail gas through two sections of pressure swing adsorption devices, most of impurity gas is removed by the first section of pressure swing adsorption device under the conditions of no vacuum pump and low pressure, and then the hydrogen is compressed and pressurized to enter the second section of pressure swing adsorption device.
CN114073882A discloses a process technology and an apparatus for simultaneously recovering multiple gases such as hydrogen and methane from petrochemical exhaust gas. The volume percentage of hydrogen in the tail gas is 28-55%, the volume percentage of hydrocarbons in the tail gas is 30-56%, and the process technology uses a vacuum pressure swing adsorption-pressure swing adsorption composite integrated device, and comprises the following steps: (a) hydrocarbon gas-vacuum pressure swing adsorption stage: separating a hydrocarbon gas product gas from the tail gas and producing an intermediate gas using a vacuum pressure swing adsorption unit; (b) a hydrogen-pressure swing adsorption stage: separating a hydrogen product gas from said intermediate gas produced in step (a) using a pressure swing adsorption unit. The process technology can simultaneously produce high-purity hydrogen, hydrocarbon gas and carbon-rich fuel gas with higher heating value.
In view of the high impurity hydrogen feed gas, and the requirement for higher purity of the product hydrogen, a new process is needed to treat the feed gas to produce high purity hydrogen.
Disclosure of Invention
The invention aims to solve the technical problem that high-purity hydrogen cannot be obtained by the conventional method, and provides a system for purifying hydrogen by two-stage pressure swing adsorption, a method for purifying hydrogen and application of the system.
In order to solve the technical problem, the invention provides a system for purifying hydrogen by two-stage pressure swing adsorption, which comprises a compressor, a first-stage pressure swing adsorption device and a second-stage pressure swing adsorption device which are sequentially connected.
Due to the increasing demand of hydrogen energy, the demand of purifying various hydrogen-containing gases in industry is increasing, and the demand is directed to the hydrogen quality (H) in the market 2 Less than 90 percent of the product hydrogen has high purity (the purity of fuel hydrogen and the product hydrogen is required), and when the recovery rate of the hydrogen has high requirement, the purification process route is comprehensively considered.
The Pressure Swing Adsorption (PSA) apparatus according to the present invention is an apparatus that adsorbs a gas under a specific pressure by utilizing the adsorption selectivity of a solid adsorbent to different gases and the characteristic that the amount of adsorption of the gas on the adsorbent changes with the change in pressure, and then separates the gas from which the adsorbed gas is desorbed by reducing the partial pressure of the adsorbed gas. The adsorption tower (filled with adsorbent) is generally nonstandard equipment, and the material and the size are selected according to the air quantity, the gas quality and the product requirement. Further, the pressure swing adsorption unit used in the process of the present invention is a fast cycle pressure swing adsorption unit (rPSA) unique to Reinecke purification plant (Shanghai) Co., ltd.
The PSA is selected in the invention without membrane or other separation equipment because:
(1) The purity of the PSA product is highly adjustable, and multiple impurity components (different adsorbents are only needed to be selected for different impurities) are removed simultaneously by one-time separation, so that the applicability is high;
(2) The PSA pressure loss is not large, the first-stage PSA product gas can directly enter the second-stage PSA, a compressor is not needed for re-pressurization, and energy is saved. In addition, the tail gas of the secondary PSA has higher hydrogen content and recovery economy, so the tail gas is mixed with the feed gas before being sent back to the inlet of the feed gas compressor, thus the hydrogen recovery rate can be obviously improved, and the recovery rate can be improved by at least 10 percent (compared with no reflux) through theoretical iterative calculation, so that the total recovery rate is more than or equal to 80 percent. If only one-stage PSA is used, the product purity requirement may not be met or the yield is extremely low. In practice the secondary PSA size will also be smaller than the primary PSA size.
In the present invention, the content of hydrogen in the raw material gas is 90% or less, and purification to 99.9% or more is required. The gas refers to the composition of the gas.
Preferably, the compressor is a diaphragm compressor; the compression ratio of the compressor is 2-3.
Preferably, the one-stage pressure swing adsorption unit is a fast cycle pressure swing adsorption unit.
Preferably, the two-stage pressure swing adsorption unit is a fast cycle pressure swing adsorption unit.
Preferably, the control valves in the first stage pressure swing adsorption unit and the second stage pressure swing adsorption unit are electrically driven rotary valves.
In the invention, the control valve for switching the adsorption time sequence of each tower body by the rPSA adopts the electric drive rotary valve, so that the loss caused by the stop of a factory and the overhaul due to the damage of an actuator sealing ring caused by frequent switching of the traditional pneumatic switch valve can be avoided, and the reliability of the whole pressure swing adsorption unit is improved.
Because an advanced and conveniently controlled electric drive rotary valve (the rotary valve is a pressure swing adsorption stepless control valve group disclosed in application No. 2020218317229) is adopted, the rPSA has the following advantages:
(1) The rotary valve has longer service life and is more reliable, and the operation verification of more than 200 sets of biogas, hydrogen and helium purifying devices for more than 3000 ten thousand hours is carried out;
(2) The reliability of the rotary valve is up to more than 99%, so that the availability of the device is up to more than 96%, and the annual operation can be stably carried out for over 8400 hours;
(3) The rotary valve has high reliability, the inspection and replacement cycle of the sealing gasket is about 5 years, and the inspection and replacement cycle is far lower than the inherent maintenance amount of the traditional pneumatic program control valve;
(4) Due to the fast cycle characteristic brought by the rotary valve, the device is reduced, the occupied area is only about 1/4 of that of the traditional PSA, and the construction investment is reduced;
(5) Due to the fast cycle characteristic brought by the rotary valve, the device is reduced, and the weight is only about 1/5 of that of the traditional PSA;
(6) Because of the fast cycle characteristic brought by adopting the rotary valve, the dynamic adsorption characteristic of the adsorbent developed by us is brought into play;
(7) The rotary valve is driven by a frequency conversion motor with extremely low power (< 500W), and a large amount of instrument air is saved compared with 30 to 50 pneumatic program control valves of the traditional PSA (each pneumatic valve needs about one instrument air in one hour);
(8) The rotary valve is driven by a variable frequency motor, so that the period adjustment is very simple, convenient and reliable, and the rotation speed single-variable adjustment control of the rotary valve can be realized by utilizing the difference between the measured value of the product gas concentration and the required set value;
therefore, rPSA has the advantages of simple operation, high reliability, small floor area, low energy consumption, high automation degree and the like compared with the traditional PSA. The application has the advantages that the whole purification process is simple and convenient to operate, the automation degree is high, and the actual industrial production is facilitated.
In a second aspect, the present invention provides a method for purifying hydrogen by the system for purifying hydrogen by two-stage pressure swing adsorption according to the first aspect, the method comprising the steps of:
(1) Introducing raw material gas into a compressor, compressing, conveying to a first-stage pressure swing adsorption device, carrying out primary purification to obtain primary product gas and primary tail gas, and directly discharging the primary tail gas from the system;
(2) And (3) conveying the primary product gas obtained in the step (1) to a secondary pressure swing adsorption device for secondary purification to obtain a final product gas, simultaneously generating secondary tail gas, and purifying again after the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
In the preparation process, no special requirements are made on the gas flow rate and the temperature. The gas flow rate may be adjusted by a person skilled in the art by conventional techniques, as long as the flow rate meets the requirements of the relevant specifications of the chemical industry, for example, the flow rate is below 15m/s, which is common for carbon steel. The temperature is generally maintained at 50 ℃.
In the invention, the yield of the product gas is greatly improved just by the process of two-stage pressure swing adsorption zone reflux, namely, the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
Preferably, the compressing in step (1) is compressing the feed gas to a pressure of 0.6MPaG to 3MPaG. For example, it may be 0.6MPaG, 1MPaG, 1.5MPaG, 2MPaG, 2.5MPaG, or 3MPaG.
In the present invention, the pressure cannot be higher than 3MPaG and not lower than 0.6MPaG, and the most preferable pressure is 1.7MPaG. Within the pressure range, the adsorbent has excellent adsorption capacity, and the purity and yield of the product gas cannot be ensured if the adsorbent is not in the pressure section.
Preferably, the process of the first-stage pressure swing adsorption device for primary purification in step (1) sequentially comprises adsorption, pressure equalization, regeneration and pressurization.
Preferably, the flow of the secondary purification performed by the two-stage pressure swing adsorption device in the step (2) sequentially comprises adsorption, pressure equalization, regeneration and pressurization.
The processes of adsorption, pressure equalization, regeneration and pressurization are specifically as follows:
(1) Adsorption
The mixed gas inlet gas flows upward through the adsorbent. In rPSA, different adsorbent beds are used, each selectively removing, for example, N from the bottom to the top of the bed 2 、CO 2 、CH 4 、CO、 H 2 O and other impurities to obtain high-purity product gas. The Reinecke engineering team will complete the bed optimization analysis to optimize the bed filling plan and obtain the best performance of the rPSA unit.
(2) Pressure equalizing
At the end of the adsorption step, the gas stored in the adsorbent of that bed is transferred to the adsorbent of another bed to recover the gas for re-pressurization/purging of the adsorbent in the other bed, which can improve system performance and save energy.
(3) Regeneration
After the pressure equalization step, the adsorbent is regenerated in three basic steps:
and (3) countercurrent purging: the adsorbent is decompressed to tail gas pressure in a countercurrent mode to remove impurities;
internal gas purging: counter-currently purging the adsorbent with stored gas from the interior of the other adsorbent bed at the pressure of the tail gas;
product gas purging: the adsorbent is purged counter-currently with product gas under tail gas pressure to fully regenerate the adsorbent.
(4) Pressure boost
At the end of the regeneration step, the regenerated adsorbent (using the stored gas in the other adsorbent beds) is pressurized by a two/three-step pressure equalization to recover a substantial portion of the stored gas. After the step is finished, the adsorption bed enters a repeated adsorption period and purifies the inlet air.
The existing recovery method, for example, the method for recovering and purifying hydrogen from semi-coke tail gas disclosed in CN113200518A, needs two times of compression, and the tail gas produced by the second pressure swing adsorption has a high hydrogen content, so that a good recovery and utilization effect cannot be achieved. Compared with the method, firstly, the rPSA used in the method has small pressure loss, generally only 0.05MPaG, and the product gas from the primary PSA can enter the secondary PSA for continuous purification without secondary compression; secondly, the method has the advantages that the whole process is optimized more obviously, the hydrogen content in the tail gas of the secondary PSA is still high, the tail gas is directly mixed with the tail gas of the primary PSA (the hydrogen content is reduced after mixing), the tail gas of the secondary PSA is recycled in the process, the tail gas of the secondary PSA returns to the initial stage and is mixed with the raw material gas to enter the compressor, the dynamic balance is finally achieved, and the yield of the method is higher than that of the method and the energy consumption is lower under the same condition.
In addition, in other prior art methods, such as the method disclosed in CN114073882A, the adopted device is still the conventional programmable valve control, and the control valve used in the present application is a highly integrated rotary valve, the control is simple and easy to operate (only the rotating speed of the rotary valve needs to be adjusted to adjust the corresponding yield and purity), and only 180s is needed to complete a complete cycle.
In a third aspect, the present invention provides a use of the system according to the first aspect for purifying hydrogen from a mixture.
The invention has the following beneficial effects:
according to the invention, through the combination of two-stage pressure swing adsorption devices, the high-impurity and low-hydrogen-containing feed gas is finally treated and subjected to iterative calculation, so that the yield of hydrogen can be more than or equal to 80% while the high-purity product hydrogen is met, and compared with the method of directly using one pressure swing adsorption device, the yield is improved by at least 10%.
Compared with the traditional PSA technology, the invention occupies compact scale of facilities, can be skid-mounted and can be controlled to be 4 meters in height; the control performance adopts a unique rotary valve group, the product gas purity feedback is adopted to control the rotating speed of the rotary valve, the full-automatic smooth 'stepless' adjustment is really realized, and the starting time is less than 20 minutes; the whole risk control is better, the tolerance to VOC is high during the operation, the gas quality can be permanently guaranteed to be qualified due to the adoption of the deviation feedback control of the gas quality of the product and a set value, the operation is fully automatic, the labor cost is reduced, the air consumption of the instrument is only about 2NCMH, and the consumption of a desulfurizer and active carbon is low.
Drawings
FIG. 1 is a schematic flow chart of a system for purifying hydrogen by two-stage pressure swing adsorption, which is provided in example 1 of the present invention.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
In the following examples of the invention, the feed gas consisted of a gas containing 1000NCMH, 65% hydrogen and 35% nitrogen.
Example 1
This embodiment provides a system of second grade pressure swing adsorption purification hydrogen
The system provided by the embodiment comprises a diaphragm compressor, a first-stage fast-cycle pressure swing adsorption device and a second-stage fast-cycle pressure swing adsorption device which are sequentially connected.
The specific method for purifying hydrogen comprises the following steps:
(1) Introducing the raw material gas into a compressor at the pressure of 2MPaG, compressing, conveying to a first-stage fast-period variable-pressure absorption device, purifying for the first time to obtain a first product gas and a first tail gas, and directly discharging the first tail gas from the system;
(2) And (2) conveying the primary product gas obtained in the step (1) to a secondary quick-period variable-pressure absorption device for secondary purification to obtain final product gas hydrogen, simultaneously generating secondary tail gas, and purifying again after the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
Example 2
This embodiment provides a system of second grade pressure swing adsorption purification hydrogen
The system provided by the embodiment comprises a diaphragm compressor, a first-stage fast-period pressure swing adsorption device and a second-stage fast-period pressure swing adsorption device which are sequentially connected.
The specific method for purifying hydrogen comprises the following steps:
(1) Introducing the raw material gas into a compressor, compressing the raw material gas at the pressure of 3MPaG, conveying the compressed raw material gas into a first-stage fast-period variable-pressure adsorption device for primary purification to obtain primary product gas and primary tail gas, and directly discharging the primary tail gas out of the system;
(2) And (2) conveying the primary product gas obtained in the step (1) to a secondary quick-period pressure swing adsorption device for secondary purification to obtain final product gas hydrogen, simultaneously generating secondary tail gas, and purifying again after the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
Example 3
This embodiment provides a system of second grade pressure swing adsorption purification hydrogen
The system provided by the embodiment comprises a diaphragm compressor, a first-stage fast-cycle pressure swing adsorption device and a second-stage fast-cycle pressure swing adsorption device which are sequentially connected.
The specific method for purifying hydrogen comprises the following steps:
(1) Introducing the raw material gas into a compressor, compressing the raw material gas at 0.6MPaG, conveying the compressed raw material gas into a first-stage fast-cycle pressure swing adsorption device for primary purification to obtain primary product gas and primary tail gas, and directly discharging the primary tail gas out of the system;
(2) And (2) conveying the primary product gas obtained in the step (1) to a secondary quick-period pressure swing adsorption device for secondary purification to obtain final product gas hydrogen, simultaneously generating secondary tail gas, and purifying again after the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
Example 4
This example differs from example 1 only in that the fast cycle pressure swing adsorption unit used in example 1 was replaced with a pressure swing adsorption unit to obtain hydrogen as a final product gas.
Example 5
The only difference between this example and example 1 is that the compressor pressure in step (1) in this example is 5MPaG, and the final product gas hydrogen is obtained.
Example 6
The only difference between this example and example 1 is that the compressor pressure in step (1) in this example is 0.2MPaG, and the final product gas, hydrogen, is obtained.
Example 7
The only difference between this example and example 1 is that the compressor pressure in step (1) in this example is 1.7MPaG, and the final product gas, hydrogen, is obtained.
Comparative example 1
The difference between the comparative example and the example 1 is that the final product gas hydrogen is obtained by purification only by using a first-stage pressure swing adsorption device and not by using a second-stage pressure swing adsorption device.
The hydrogen provided in the above examples was subjected to purity and overall recovery tests, the specific results are shown in table 1 below:
TABLE 1
As can be seen from the data in Table 1, the present invention can achieve the best yield at the optimum pressure, i.e., 1.7MPaG, and the yield can reach 87.5%. If only one-stage pressure swing adsorption is used, and no two-stage pressure swing adsorption and reflux process is adopted, the yield is reduced to only 70 percent. When the method is considered within the range defined by the invention, the process flow is optimal, and the yield is highest. If the pressure is too high or too low, the method cannot be applied to an actual production process, and has no actual application value.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (10)
1. A system for purifying hydrogen by two-stage pressure swing adsorption is characterized by comprising a compressor, a first-stage pressure swing adsorption device and a second-stage pressure swing adsorption device which are sequentially connected.
2. The system of claim 1, wherein the compressor is a diaphragm compressor; the compression ratio of the compressor is 2-3.
3. The system of claim 1 or 2, wherein the primary pressure swing adsorption device is a fast cycle pressure swing adsorption device.
4. The system of any of claims 1-3, wherein the two-stage pressure swing adsorption device is a fast cycle pressure swing adsorption device.
5. The system of any of claims 1-4, wherein the control valves in the primary pressure swing adsorption unit and the secondary pressure swing adsorption unit are electrically driven rotary valves.
6. The method for purifying hydrogen by the system for purifying hydrogen by two-stage pressure swing adsorption according to any one of claims 1 to 5, wherein the method comprises the steps of:
(1) Introducing raw material gas into a compressor, compressing, conveying to a first-stage pressure swing adsorption device, carrying out primary purification to obtain primary product gas and primary tail gas, and directly discharging the primary tail gas from the system;
(2) And (3) conveying the primary product gas obtained in the step (1) to a secondary pressure swing adsorption device for secondary purification to obtain a final product gas, simultaneously generating secondary tail gas, and purifying again after the secondary tail gas is returned to be mixed with the raw material gas in the step (1).
7. The method of claim 6, wherein the compressing in step (1) is compressing the feed gas to a pressure of 0.6MPaG to 3MPaG.
8. The method according to claim 6 or 7, wherein the primary purification flow of the one-stage pressure swing adsorption device in step (1) sequentially comprises adsorption, pressure equalization, regeneration and pressurization.
9. The method according to any one of claims 6 to 8, wherein the flow of the secondary purification in the two-stage pressure swing adsorption unit in the step (2) comprises adsorption, pressure equalization, regeneration and pressurization in sequence.
10. Use of a system according to any one of claims 1 to 5 for the purification of hydrogen from a gas mixture.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210982399.2A CN115253595A (en) | 2022-08-16 | 2022-08-16 | System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210982399.2A CN115253595A (en) | 2022-08-16 | 2022-08-16 | System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN115253595A true CN115253595A (en) | 2022-11-01 |
Family
ID=83750614
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202210982399.2A Pending CN115253595A (en) | 2022-08-16 | 2022-08-16 | System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN115253595A (en) |
Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101474520A (en) * | 2008-01-03 | 2009-07-08 | 上海标氢气体技术有限公司 | Device for adsorptive separation and purification of industrial gas |
| CN104030244A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method for recovering high-yield high-purity hydrogen gas from refinery dry gas |
| CN105347304A (en) * | 2015-12-18 | 2016-02-24 | 四川天采科技有限责任公司 | Double-high PSA (pressure swing adsorption) hydrogen purification method adopting pressure desorption |
| CN107758615A (en) * | 2016-08-22 | 2018-03-06 | 四川天采科技有限责任公司 | A kind of low energy consumption, raw coke oven gas hydrogen production process in high yield |
| CN109355120A (en) * | 2018-11-23 | 2019-02-19 | 通用绿色气体公司 | Biogas purification natural gas method |
| CN109921073A (en) * | 2019-03-14 | 2019-06-21 | 四川天一科技股份有限公司 | Anode of fuel cell gas efficiently produces the method and system of hydrogen fuel cell hydrogen |
| CN112374459A (en) * | 2020-11-26 | 2021-02-19 | 中国石油化工股份有限公司 | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery |
| CN213761173U (en) * | 2020-08-27 | 2021-07-23 | 瑞必科净化设备（上海）有限公司 | Pressure swing adsorption's stepless control valves and pressure swing adsorption equipment |
| CN113200518A (en) * | 2021-06-11 | 2021-08-03 | 西南化工研究设计院有限公司 | Method for recovering and purifying hydrogen from semi-coke tail gas |
| CN114408860A (en) * | 2021-12-31 | 2022-04-29 | 西南化工研究设计院有限公司 | Efficient and energy-saving ammonia cracking hydrogen production method |
-
2022
- 2022-08-16 CN CN202210982399.2A patent/CN115253595A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101474520A (en) * | 2008-01-03 | 2009-07-08 | 上海标氢气体技术有限公司 | Device for adsorptive separation and purification of industrial gas |
| CN104030244A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method for recovering high-yield high-purity hydrogen gas from refinery dry gas |
| CN105347304A (en) * | 2015-12-18 | 2016-02-24 | 四川天采科技有限责任公司 | Double-high PSA (pressure swing adsorption) hydrogen purification method adopting pressure desorption |
| CN107758615A (en) * | 2016-08-22 | 2018-03-06 | 四川天采科技有限责任公司 | A kind of low energy consumption, raw coke oven gas hydrogen production process in high yield |
| CN109355120A (en) * | 2018-11-23 | 2019-02-19 | 通用绿色气体公司 | Biogas purification natural gas method |
| CN109921073A (en) * | 2019-03-14 | 2019-06-21 | 四川天一科技股份有限公司 | Anode of fuel cell gas efficiently produces the method and system of hydrogen fuel cell hydrogen |
| CN213761173U (en) * | 2020-08-27 | 2021-07-23 | 瑞必科净化设备（上海）有限公司 | Pressure swing adsorption's stepless control valves and pressure swing adsorption equipment |
| CN112374459A (en) * | 2020-11-26 | 2021-02-19 | 中国石油化工股份有限公司 | System and method for improving hydrogen recovery rate in styrene dehydrogenation tail gas of oil refinery |
| CN113200518A (en) * | 2021-06-11 | 2021-08-03 | 西南化工研究设计院有限公司 | Method for recovering and purifying hydrogen from semi-coke tail gas |
| CN114408860A (en) * | 2021-12-31 | 2022-04-29 | 西南化工研究设计院有限公司 | Efficient and energy-saving ammonia cracking hydrogen production method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107789949B (en) | Gas separation method by negative pressure swing adsorption | |
| JP3553568B2 (en) | Adsorbent for separating nitrogen from oxygen / nitrogen mixed gas and method for producing nitrogen using the same | |
| CN210340328U (en) | Integrated continuous oxygen and nitrogen making device | |
| KR930010571B1 (en) | Purifying combustible gases containing carbon monoxide | |
| CN1083731C (en) | Simulataneous step pressure swing adsorption process | |
| EP1101522B1 (en) | Pressure swing adsorption process | |
| KR102481433B1 (en) | Method of Separating and Purifying Hydrogen from Gas Mixture of Ammonia Decompositions | |
| KR20090091327A (en) | Hydrogen adsorption purification method with co-generation of a pressurised co2 flow | |
| CN202569898U (en) | Nitrogen producing device | |
| CN109126381B (en) | Method for removing carbon dioxide in industrial gas through pressure swing adsorption | |
| CN113350968A (en) | Hydrogen extraction device and process for recovering tail gas components by using synthetic hydrogen | |
| CN113200518A (en) | Method for recovering and purifying hydrogen from semi-coke tail gas | |
| CN108236829B (en) | From the content of CO2Separation of high purity CO from raw material gas2Method and apparatus | |
| US20140069275A1 (en) | Low energy cyclic psa process | |
| CN110639328A (en) | Method for removing trace carbon impurities in tail gas recovery hydrogen treatment process | |
| CN115337758A (en) | System for purifying hydrogen through membrane separation and pressure swing adsorption, method for purifying hydrogen and application | |
| CN115253595A (en) | System for purifying hydrogen with backflow through two-stage pressure swing adsorption, method for purifying hydrogen and application | |
| CN214243809U (en) | System for producing hydrogen and coproducing LNG (liquefied Natural gas) by using raw gas | |
| CN116390797A (en) | Process and apparatus for producing ultra-high purity hydrogen from low grade hydrogen | |
| CN1618729A (en) | Technology of combined extreacting carbon dioxide and hydrogen using medium varying gas decarbonization-varying pressure adsorption | |
| CN115321484A (en) | System for purifying hydrogen by two-stage compression and adsorption, method for purifying hydrogen and application | |
| CN112374959A (en) | Method for separating ethylene and ethane in catalytic dry gas | |
| CN1040292C (en) | Gas separation method by pressure swing adsorption for simultaneously preparing two gas products with high-purity and high-yield | |
| CN220424946U (en) | Carbon dioxide purification device | |
| CN216472232U (en) | Energy-saving process system for purifying hydrogen from raw coke oven gas with low-concentration hydrogen |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |