CN117101327A - Effective energy recovery method in PSA pressure swing adsorption separation process - Google Patents
Effective energy recovery method in PSA pressure swing adsorption separation process Download PDFInfo
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- CN117101327A CN117101327A CN202210525791.4A CN202210525791A CN117101327A CN 117101327 A CN117101327 A CN 117101327A CN 202210525791 A CN202210525791 A CN 202210525791A CN 117101327 A CN117101327 A CN 117101327A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 173
- 238000000034 method Methods 0.000 title claims abstract description 71
- 238000000926 separation method Methods 0.000 title claims abstract description 69
- 238000011084 recovery Methods 0.000 title claims abstract description 58
- 238000006243 chemical reaction Methods 0.000 claims abstract description 69
- 230000008569 process Effects 0.000 claims abstract description 39
- 239000002994 raw material Substances 0.000 claims abstract description 12
- 238000005265 energy consumption Methods 0.000 claims abstract description 5
- 239000003463 adsorbent Substances 0.000 claims description 21
- 230000002441 reversible effect Effects 0.000 claims description 12
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 8
- 230000018044 dehydration Effects 0.000 claims description 8
- 238000006297 dehydration reaction Methods 0.000 claims description 8
- 239000007788 liquid Substances 0.000 claims description 8
- 230000001174 ascending effect Effects 0.000 claims description 7
- 238000001816 cooling Methods 0.000 claims description 7
- 238000007599 discharging Methods 0.000 claims description 7
- 230000008929 regeneration Effects 0.000 claims description 7
- 238000011069 regeneration method Methods 0.000 claims description 7
- 230000008859 change Effects 0.000 claims description 5
- 229910021529 ammonia Inorganic materials 0.000 claims description 4
- 239000000654 additive Substances 0.000 claims description 2
- 230000000996 additive effect Effects 0.000 claims description 2
- 238000010926 purge Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 104
- 238000004458 analytical method Methods 0.000 abstract description 3
- 229910052799 carbon Inorganic materials 0.000 abstract description 3
- 238000004364 calculation method Methods 0.000 abstract description 2
- 239000002918 waste heat Substances 0.000 abstract description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 26
- 229910052739 hydrogen Inorganic materials 0.000 description 19
- 239000001257 hydrogen Substances 0.000 description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 15
- 238000004519 manufacturing process Methods 0.000 description 11
- 238000010586 diagram Methods 0.000 description 10
- 239000003245 coal Substances 0.000 description 5
- 239000012071 phase Substances 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 229910052757 nitrogen Inorganic materials 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- JVFDADFMKQKAHW-UHFFFAOYSA-N C.[N] Chemical compound C.[N] JVFDADFMKQKAHW-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000002194 synthesizing effect Effects 0.000 description 2
- 229910000838 Al alloy Inorganic materials 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 239000002925 low-level radioactive waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
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- 238000005457 optimization Methods 0.000 description 1
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- 229910052760 oxygen Inorganic materials 0.000 description 1
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- 238000007670 refining Methods 0.000 description 1
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- 230000001172 regenerating effect Effects 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K13/00—General layout or general methods of operation of complete plants
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
- F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
- F01K27/00—Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
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- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
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- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
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Abstract
The effective recovery method in PSA pressure swing adsorption separation process can be known from analysis and calculation of effective energy of inlet and outlet gas of PSA pressure swing adsorption separation process equipment, in particular, the adsorption phase content is high, for example, the conversion gas CO of H2 produced from high-carbon raw material 2 When the pressure of the equal-pressure mixed gas is above 1MPa, the loss of the effective efficiency of the inlet gas and the outlet gas of the PSA pressure swing adsorption separation process system is not negligible. By arranging the air flow energy recovery device in the related pipeline, the energy released by the air flow under the pressure difference condition is converted into mechanical energy, and then the mechanical energy is converted into electric energy through the connected motor, so that the effective energy recovery in the PSA pressure swing adsorption separation process can be realized. At the same time, the air flow can be increased by adopting low-position waste heat to heat the air flowThe effective recovery, or the effective recovery is used for controlling the temperature of the adsorption bed layer, or the low-temperature airflow is used for reducing the temperature of the adsorption bed layer and the product gas, so that the energy consumption of the subsequent process is reduced, or the cold energy is provided for other working procedures.
Description
Technical Field
The invention belongs to the field of chemical industry, and in particular relates to a technical method for effectively recycling process airflow in the adsorbent regeneration process in a gas PSA pressure swing adsorption separation process.
Background
In the production of synthesis gas or hydrogen from coal, oil, natural gas, etc., CO is usually provided 2 And (3) removing and separating. Because the separated medium has no gas or liquid phase in the PSA pressure swing adsorption separation processThe change is carried out, the high-low pressure and high-low temperature circulation of the solution is avoided, the inlet of the bed with the largest process temperature change is basically in the normal temperature range of 5-50 ℃, and the outlet temperature of the bed is basically unchanged; the separation process does not need or consumes little energy, has no process waste liquid, and has the advantages of high automation degree and the like. The process has been successfully developed since the 1960 s of the last century and has begun industrial application. The method is widely applied to gas separation processes in industries such as global synthesis ammonia, methanol, oil refining and the like.
The PSA pressure swing adsorption separation process can also be applied to the mixture separation of various gases such as oxygen production by air separation, nitrogen production, hydrogen production by coal, hydrogen methane separation and the like.
PSA pressure swing adsorption separation processes typically involve the adsorption of substances such as CO by adsorbents 2 The adsorption amount is directly proportional to the partial pressure, and the easily adsorbed component is adsorbed from the mixed gas with adsorbent under relatively high pressure, and the non-adsorbed or difficultly adsorbed gas is H 2 Under the pushing of the pressure difference of the air flow, the air flow is pushed out of the adsorbent bed layer and the adsorption tower from the gaps among the adsorbent particles, so that the components such as H which are not easy to be adsorbed are realized 2 Separating from the mixture thereof; then under the condition of relatively low pressure, the adsorption quantity and the proportional relation of the pressure are utilized to adsorb the components such as CO 2 Desorbing and releasing the desorbed component such as CO into the space by pushing with the pressure difference of the gas flow 2 Sending the mixture into another space to realize the regeneration of the adsorbent, and leading the adsorbent to absorb CO again under the condition of high pressure 2 Is a performance of the (c).
From analysis and calculation of effective energy of inlet and outlet gases of PSA pressure swing adsorption separation process device, it is known that, in particular, H is prepared from high-carbon raw material 2 Is converted into CO 2 The content of the CO is more than 30 percent, even the CO is contained 2 The loss of the effective efficiency of the inlet and outlet gases of the PSA pressure swing adsorption separation process device is not negligible when the mixed gas pressure is 1MPa or even more than 4 MPa. For example, a large CTL coal-to-oil production line is being designed, which produces H 2 Pressure swing adsorption hydrogen production by pressure PSA at 3MPaProcess, device inlet gas total amount reaches 660000Nm 3 /h, wherein CO 2 The content reaches 45 percent, and the outlet H 2 The gas content is more than or equal to 99.9 percent, and the gas quantity is 340000Nm 3 And/h, the effective efficiency loss of the PSA separation process reaches 33000 kwh/above. The effective energy of 264kwh is directly lost in the PSA process only when one ton of fuel oil is produced, and CO is increased 2 211kg were discharged.
CN205832901U is a pressure swing adsorption system residual pressure residual energy recycling device, is connected to a main air pipe through an analysis air pipe and a reverse air release pipe, and is connected with a turbine after passing through a preheating pipe, and the turbine is connected with a generator to recycle residual pressure. Because the reverse desorption suction pressure is reduced by 90 percent, even more than 99 percent compared with the inlet pressure of the PSA device, most of the original pressure effective performance is dissipated in the molecular thermal motion of the air flow in the pressure equalizing and forward releasing process and is conducted to the contacted substances (adsorbent, components and walls) to be lost, and the substances are not recovered at all. Even if the heating pipe is arranged to heat the gas, the effective energy of the gas is increased, and the reverse desorption gas pressure is low, and the gas quantity is small, so that the effective energy recovery is very limited, and the thought, the mode and the device for recovering and utilizing the residual energy have not been paid attention in the industry.
CN101285638B utilizes the semi-open type coalbed methane nitrogen expansion liquefaction process of pressure swing adsorption residual pressure, CN101285639B utilizes the coalbed methane nitrogen expansion liquefaction process of pressure swing adsorption residual pressure precooling, and only the high-pressure potential energy of non-adsorption phase nitrogen which is discharged into the atmospheric environment after being discharged out of the tower is recycled, adiabatic expansion refrigeration is carried out through an expander, and the effective energy of the air flow lost in the pressure swing adsorption pressure equalizing, forward discharging and final flushing process is not recycled, so that process optimization and energy recovery are carried out.
A gas is adsorbed, essentially by the attractive forces that exist between the adsorbent micro-electromagnetic structure and the adsorbed gas micro-electromagnetic structure, and the amount of adsorbed is proportional to its partial pressure at a given temperature. The pressure swing adsorption separation process utilizes the characteristic, and the partial pressure found by daltons is in direct proportion to the volume fraction, namely the law of daltons partial pressure; by adopting a special technological process, the partial pressure of the container filled with the specific adsorbent can be orderly changed by changing the pressure in a plurality of containers which are communicated with each other and can be separated, and the volume fraction of the mixed gas can be changed, so that the continuous separation of the mixed gas is realized.
The mixed gas is separated in the adsorption bed under isothermal condition, the heat release of the adsorption phase is almost absorbed by the adsorbent, and the mass of the adsorbent is far greater than that of the mixed gas in an adsorption separation period, (2) the adsorption phase is mainly concentrated in the lower half part of the adsorption bed layer, so that the temperature rise of the general medium adsorption process, especially the outlet of the adsorption tower, is negligible in the general industrial process design.
In industrial processes, whether PSA isothermal separation, cryocondensation separation, or solvent physical/chemical absorption separation, membrane separation processes, the minimum separation work required for gas separation is typically provided by the mixed gas at the inlet of the separation device. But is just high CO such as hydrogen production by coal, ammonia production by coal, and the like 2 In the PSA separation process, the process gas does not have phase change liquefaction with greatly reduced volume, and key physical conditions are provided for greatly recovering energy loss in the decompression separation process.
Disclosure of Invention
The invention aims to provide a technical method for the society, which can directly convert a large proportion of effective energy lost in the traditional PSA pressure swing adsorption separation process into mechanical energy and electric energy and obtain a cryogenic pressure swing adsorption process with low temperature even below-100 ℃.
An effective recovery method in a PSA pressure swing adsorption separation process, characterized by: in the effective gas recovery and additive regeneration process in the adsorption tower of the PSA pressure swing adsorption separation process, arranging a gas flow energy conversion device (TP) in a channel for discharging gas from the adsorption tower and the container with relatively high pressure to the adsorption tower and the container with relatively low pressure, converting the energy of the gas flow from the adsorption tower and the container with relatively high pressure into mechanical energy, and converting the mechanical energy into electric energy through a connected generator (FD), as shown in FIG. 12;
a heater (JRQ) is arranged in an air inlet pipeline of the airflow energy conversion device (TP) so as to heat the airflow and increase the effective energy obtaining amount of the airflow;
the low-temperature gas expanded by the airflow energy conversion device (TP) is used for working, the bed temperature of the other adsorption tower is reduced, the adsorption capacity is improved, the volume of the adsorbent is reduced, and the temperature of a separated product is reduced;
feeding cold energy back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ) by using low-temperature high-pressure product Gas (GYCPQ), and reducing the bed temperature of the adsorption tower and the low-temperature low-pressure product gas (DYCPQ) to lower temperature;
similarly, the low-pressure product gas with low temperature is fed back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ), so that the bed temperature of the adsorption tower and the high-pressure product Gas (GYCPQ) are reduced to lower temperature;
the low-temperature high-pressure product Gas (GYCPQ) and the low-temperature low-pressure product gas (DYCPQ) are fed back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ), so that the temperature of the adsorption tower bed layer is reduced, and simultaneously, the pressure of the pressure swing adsorption process, the pressurizing energy consumption of the raw material gas and the CO produced by energy sources are reduced 2 Discharging;
in the pressure swing adsorption process provided with a plurality of airflow energy conversion devices (TP), the cold energy of the outlet air of each airflow energy conversion device (TP) is concentrated and output to a cooling device by adopting a circulating cold-conducting liquid serial cold exchange circulation mode, as shown in FIG. 11;
the cold obtained by the pressure swing adsorption process provided with the airflow energy conversion device (TP) is exchanged to another set of pressure swing adsorption process device or ammonia cooling device or other devices such as air cryogenic separation devices requiring low temperature through dividing wall heat exchange or liquid circulation mode, so that the process temperature can be reduced.
2. The method for recovering the effective energy in the PSA pressure swing adsorption separation process is characterized in that the uniform descending air flows from the adsorption tower (A) to the adsorption tower (H) in the same circulation, all of which flow into a uniform descending air flow energy conversion device (TP 1) after passing through a uniform descending main pipe (1 JJZG) in order, and flow into the corresponding adsorption tower after passing through a uniform ascending main pipe (1 JSZG) in order, see the attached figure 1;
the two uniform descending air flows from the adsorption tower (A) to the adsorption tower (H) in the same circulation flow into the two uniform descending air flow energy conversion device (TP 2) after passing through the two uniform descending main pipes (2 JJZG) in order, and flow into the corresponding adsorption towers after passing through the two uniform ascending main pipes (2 JZG) in order, see the attached figure 1;
the three-average descending air flows from the adsorption tower (A) to the adsorption tower (H) in the same circulation flow into the three-average descending air flow energy conversion device (TP 3) after passing through the three-average descending main pipe (3 JJZG) in order, and flow into the corresponding adsorption tower after passing through the three-average ascending main pipe (3 JZG) in order, see the attached figure 1;
when the system pressure is high, the pressure equalizing times will exceed 3 times, namely the N-th uniform pressure drop air flow of the adsorption towers in the same cycle passes through the N-th uniform descending main pipe in sequence, then flows into the N-th uniform descending air flow energy conversion device, and flows into the corresponding adsorption towers after passing through the N-th uniform ascending main pipe in sequence, wherein the number of the adsorption towers in the same cycle is less than or equal to 50.
3. The method for effectively recovering the energy in the PSA pressure swing adsorption separation process is characterized in that an air flow energy conversion device (TP) directly arranged at an inlet and outlet pipeline at the top of the adsorption tower can convert the energy of the air flow flowing into the adsorption tower into mechanical energy and the energy of the air flow flowing out of the adsorption tower into mechanical energy (see figures 9 and 10); the airflow energy conversion device (TP) arranged on the inlet and outlet pipelines at the top of the adsorption tower is provided with a bypass one-way valve, only the energy of the airflow entering the tower can be converted into mechanical energy (see figure 7), and the airflow exiting the tower does not flow out of the adsorption tower through the airflow energy conversion device (TP) (see figure 8).
4. The method for effectively recovering the efficiency in the PSA pressure swing adsorption separation process is characterized in that a generator (FD) connected with a gas flow energy conversion device (TP) is changed into a motor generator, and electric energy can be input to drive the gas flow energy conversion device (TP) at the later stage of a pressure equalization period, so that the gas flow speed is increased, the pressure equalization time is shortened, and the pressure swing adsorption cycle period is further shortened.
5. The effective energy recovery method in the PSA pressure swing adsorption separation process is characterized in that the method is arranged in a rotating impeller of an airflow energy conversion device (TP) in the middle part (see figure 3 of the specification) of a pressure equalizing main pipe (1 JYZG), a two pressure equalizing main pipe (2 JYZG), a three pressure equalizing main pipe (3 JYZG), an N times pressure equalizing main pipe (NLYZG) and a forward-putting main pipe (SFZG) and is unidirectionally rotated, and airflows at two ends of the airflow energy conversion device (TP) are introduced in the rotating direction of the impeller (see figures 4 and 5) to transfer energy to the impeller to be converted into mechanical energy; the bleed air flows of the adsorption tower (A, B, C, D) and the adsorption tower (E, F, G, H) at the two ends of the air flow energy conversion device (TP) are respectively and sequentially sent to the adsorption tower at the other end through the air flow energy conversion device (TP) by program control; the number of the adsorption towers is less than or equal to 50; n in the N times equalizing manifold (nJYzg) includes the forward manifold: an integer of 1.ltoreq.N.ltoreq.16.
6. The method for effectively recovering the energy in the PSA pressure swing adsorption separation process is characterized in that the temperature of the bed layer of the adsorption tower is controlled by adjusting the temperature of a heater (JRQ) and the energy conversion efficiency of a gas flow energy conversion device (TP).
7. The effective energy recovery method in the PSA pressure swing adsorption separation process is characterized in that the check valve positions (see fig. 4 and 5) arranged at the inlet and the outlet of the airflow energy conversion device (TP) are controlled, so that when the two ends of the airflow energy conversion device (TP) are alternately charged, the air is introduced along the rotation direction of the impeller, and the unidirectional rotation of the turbine impeller is realized; and the impeller shaft and the flywheel are used for storing energy by inertia, so that the electric power amplitude caused by air flow pressure difference and flow change is reduced.
8. The method for effectively recovering the energy in the PSA pressure swing adsorption separation process is characterized in that a gas flow energy conversion device (TP) is arranged in a tower bottom pressure equalizing main pipe (TDJYZG) of an adsorption tower and a reverse gassing main pipe (NFQZG) for energy recovery.
9. The method for effectively recovering the energy in the PSA pressure swing adsorption separation process is characterized in that in the same circulation flow, a gas flow energy conversion device (TP) is arranged in a pressure equalizing pipeline at the top of an adsorption tower, a pressure equalizing pipeline at the bottom of the adsorption tower, a discharge gas pipeline at the bottom of the adsorption tower and a final pressure boosting main pipe for energy recovery.
10. The method for recovering the effective energy in the PSA pressure swing adsorption separation process is characterized in that a gas flow energy conversion device (TP) and a heater (JRQ) are arranged in a pressure equalizing pipeline of the temperature swing adsorption separation process, so that the effective energy in the discharged gas is recovered and the temperature of a temperature swing adsorption bed layer is controlled.
The invention has the following positive effects:
the invention can be adopted to effectively recycle the lost effective energy in the traditional PSA pressure swing adsorption separation process, especially the industrial device with higher adsorption phase content or high purity requirement of separation products or larger scale or higher pressure or the temperature of an adsorption bed layer to be reduced; by recovering the lost effective energy (effective energy) in the separation process, the energy loss is reduced, the energy efficiency of the PSA process is improved, and the CO produced by energy is further reduced 2 And (5) discharging.
The low-temperature high-pressure product Gas (GYCPQ) is fed back to the dehydration raw gas (TSYLQ) through a cold exchanger (LJHQ), as the dehydration raw gas does not have water vapor adsorption, condensation and heat release, the pressure reduction, regeneration and heat release of the adsorbent are greatly reduced according to heat balance, so that the temperature of the gas entering a gas flow energy conversion device (TP) is reduced, the temperature is lower after the adiabatic expansion of a turbine, particularly the gas under low pressure, such as four pressure and five pressure, the expansion ratio is large, the temperature reduction amplitude is large, the generated energy is reduced, but the pressure reduction process gas with lower temperature is obtained, the bed temperature of an adsorption tower and the temperature of the low-pressure product gas (DYCPQ) are reduced to be lower than 0 ℃ and even lower than-40 ℃, and the temperature of the adsorption tower bed temperature and the low-pressure product gas (DYCPQ) are reduced to produce liquid CO 2 Obviously very advantageous; in particular, the cold energy obtained by the pressure swing adsorption device provided with the airflow energy conversion device (TP) is exchanged to another pressure swing adsorption device provided with the airflow energy conversion device (TP), so that the pressure swing adsorption device receiving the cold energy can be realized, the pressure swing adsorption process temperature of the deep low temperature below-100 ℃ is lower, and the energy consumption of the subsequent liquid process is obviously reduced for low-pressure product gas such as methane products to be liquefied in the subsequent process.
The cold energy of the low-temperature product gas with high pressure and low pressure is fed back to the raw material gas, so that the temperature of the low-heat-release pressure-swing adsorption process can be obtained, the adsorption capacity of the adsorbent can be increased, the using amount of the adsorbent can be reduced, the pressurizing pressure energy consumption of the raw material gas can be reduced, and the investment of the device can be reduced.
Due to the installation of the airflow energy conversion device (TP), not only is energy recovered, but also due to the fact that the pipeline bears the function of converting airflow pressure difference into mechanical energy, the related pipeline valves are all enlarged in cross section area, so that the initial pressure difference of average pressure drop and the resistance of the airflow pipeline are greatly reduced, the energy recovery rate is greatly improved, the strong impact of the average pressure difference on the adsorbent and the valve is also greatly reduced, the pulverization and the operation resistance increase of the adsorbent are effectively prevented, the damage rate of the valve is reduced, the service time of the adsorbent and the valve is prolonged, and the separation process cost is reduced; the structures of the distributor and the compacting device at the top and the bottom of the adsorbent bed can be greatly simplified, the air flow resistance is greatly reduced, and the effective recovery rate is increased;
when the generator (FD) matched with the airflow energy conversion device (TP) is changed into a motor generator, electric energy can be input to drive the airflow energy conversion device (TP) at the later stage of the pressure equalizing and reducing period, so that the airflow speed is accelerated, the pressure equalizing and regenerating time is shortened, the pressure swing adsorption cycle period is further shortened, and the productivity of the PSA device can be greatly improved.
The impeller of the airflow energy conversion device (TP) has low working temperature, and can also be made of low-cost aluminum alloy and nonmetallic materials.
Drawings
FIG. 1 is a schematic diagram of an efficient recovery turbine disposed between a common drop header and a common rise header;
FIG. 2 is a schematic diagram of an efficient recovery turbine on the top of the adsorption column or on the gas inlet and outlet lines of the top of the adsorption column;
FIG. 3 is a schematic diagram of an efficient recovery turbine disposed intermediate each of the equalization and bleed manifolds;
FIG. 4 is a schematic illustration of the turbine wheel rotating in a single direction counter clockwise with the turbine left inlet and check valve position;
FIG. 5 is a schematic illustration of the check valve position of the turbine wheel rotating in a single direction counter clockwise with the intake air at the right end of the turbine;
FIG. 6 is a schematic diagram of the recovery of the effective energy from the gas stream using dehydrated mixed gas (TSHHQ) and a pressure equalization header at the bottom of the column with a gas stream energy conversion device (TP) installed therein;
FIG. 7 is a schematic diagram showing the flow of gas into the adsorption column only through the gas flow energy conversion device (TP) when the check valve is closed;
FIG. 8 is a schematic diagram showing the flow of air out of the adsorption tower only through the opening of the bypass check valve when the check valve is opened;
FIG. 9 is a schematic diagram of the flow of gas through a turbine wheel into a pressure increasing adsorption column;
FIG. 10 is a schematic diagram of the flow of gas from the depressurization adsorption tower through the turbine wheel;
FIG. 11 is a schematic diagram of a cooling device by a circulating cold-conducting liquid serial cold exchange circulation mode, wherein the cold quantity is intensively output to the cooling device;
FIG. 12 is a schematic diagram of a gas stream energy conversion device (TP) configuration for an efficient recovery method as described herein;
the meaning of the label expression in the figure is as follows:
YLQ is a pipeline of raw gas;
GYCPQ. High pressure product gas and its pipeline;
CYNFQ normal pressure reverse-deflating and pipeline thereof;
DYCPQ. Low pressure product gas and its pipeline;
1JSZG, first uniform lift and main pipe thereof;
1JJZG, firstly reducing the gas and a main pipe thereof;
2JSZG, second uniform lift and main pipe thereof;
2JJZG, two-step reducing the gas and a main pipe thereof;
3JSZG, three-liter gas and a main pipe thereof;
3JJZG, three-all reducing gas and its main pipe;
1JYZG, a pressure equalizing gas and a main pipe thereof;
2JYZG, second equalizing gas and main pipe thereof;
3JYZG, three equalizing gases and main pipe thereof;
nJYZG.N uniform pressure gas and total pipe, integer of N is more than or equal to 1 and less than or equal to 20; n=1, namely a pressure swing adsorption separation process with only one pressure equalization;
NJZG.N is an integer of 1-20 and equal in pressure drop and total pipe; n=1, namely a pressure swing adsorption separation process with only one pressure equalization;
njszg.n equalizing and lifting and total pipe, integer N is 1-20; n=1, namely a pressure swing adsorption separation process with only one pressure equalization;
ylsb using a cooling device;
lyxhb cold night circulation pump;
SFQZG. Forward bleed and its main pipe;
nfqzg reverse bleed air and header thereof;
tdJYzg, tower bottom uniform pressure gas and main pipe thereof;
ljhq. cold exchanger;
TSYLQ dehydrated gas mixture and pipeline thereof
A. B, C, D, E, F, G, H, adsorption tower and numbering thereof;
v1, a low pressure product gas buffer tank;
zkp vacuum pump;
jrq. heater;
FD. generator;
TP. air current energy conversion device;
TP1, a uniform descent gas flow energy conversion device;
TP2, a two-average drop airflow energy conversion device;
TP3, three-average drop airflow energy conversion device;
TP4, a reverse bleed air energy conversion device;
Detailed Description
Example 1
Methane content 40%, hydrogen content 60%, air flow 200000Nm 3 And/h, a pressure of 3.0MPa (g) and a temperature of 40 ℃. The PSA pressure swing adsorption separation process of the invention is adopted for separation by an effective recovery method. The yield of the methane product is more than or equal to 98 percent, wherein the hydrogen is less than or equal to 2 percent; the yield of the hydrogen product is 98%, wherein methane is less than or equal to 2%. The methane product pressure was 0.12MPa (A) and the hydrogen product pressure was 2.9MPa. The pressure swing adsorption of single set of PSA adopts the process of 12-3-5/P with the inner diameter of 3.8 m and the total resistance drop of two sections of adsorption is less than or equal to 0.1MPa, and the pressure is equalized for 5 times and the pressure is discharged for 1 time. The main pipe is provided with an air flow energy recovery Turbine (TP), a heater (JRQ) is additionally arranged at the inlet of the air flow energy recovery Turbine (TP), and the air flow is heated by utilizing low-level waste heat of the process so as to improve the energy recovery rate:
firstly, the turbine installed power is reduced by 330kw, the average recovery power is 250kw in an hour, and the average recovery power accounts for 4.6 percent of the total recovery;
reducing the installed power of the turbine by 400kw, and recovering the electric power by 300kw in an average time, wherein the electric power accounts for 5.5% of the total recovery amount;
reducing the turbine installed power by 500kw, and recovering the electric power by 400kw in an average time, wherein the electric power accounts for 7.4% of the total recovery amount;
the turbine installed power is reduced by 700kw, the average recovery power is 550kw in an hour, and the recovery power accounts for 10.2 percent of the total recovery;
reducing turbine installed power by 1200kw, and recovering power by 900kw in an average time, wherein the power accounts for 16.7% of the total recovery amount;
the installed power of the forward-bleed turbine is 4000kw, the average recovery power is 3000kw in an hour, and the power accounts for 55.5 of the total recovery amount;
the total recovery rate of the electric power is 5400kwh/h, and the effective energy recovery rate is 65%;
example 2
Dehydrated feed gas (TSYLQ): methane content 40%, hydrogen content 60%, air flow 200000Nm 3 And/h, a pressure of 3.0MPa (g) and a temperature of 30 ℃. The PSA pressure swing adsorption separation process of the invention is adopted for separation by an effective recovery method without a heater (JRQ). The pressure swing adsorption of single set of PSA adopts the internal diameter of 3.8 m, the total resistance drop of two sections of adsorption of 12-3-5/P process is less than or equal to 0.1MPa, the regeneration adopts 5 times of pressure equalizing, 1 time of forward discharge and 1 time of reverse discharge. The reverse bleed main pipe (NFQZG) is provided with a gas flow energy recovery turbine (TP 4) for providing low-temperature methane gas for the subsequent process. The whole set of equipment pipeline is cold-insulated, and the pipeline pipe fitting of the pressure vessel adopts a low-temperature alloy material.
The yield of hydrogen (GYCPQ) was 98% and the amount of the product was 120000Nm 3 And/h, wherein methane is less than or equal to 2%, the pressure of the hydrogen product is 2.9MPa, and the hydrogen product passes through a cold exchanger (LJHQ) (see figure 6) at the temperature of 27 ℃ to take off 134kwh of cold.
The yield of methane product is more than or equal to 98 percent, and the gas flow is 80000Nm 3 And/h, wherein the hydrogen is less than or equal to 2%, the pressure of the methane product is 0.12MPa (A), the temperature is-71 ℃ (202K), and the product gas is subjected to a liquefaction step; .
The turbine installed power is reduced by 330kw, and the electric power is recovered by 170kw in an average time;
reducing the installed power of the turbine by 400kw, and recovering the electric power by 200kw in an average time;
reducing turbine installed power by 500kw, and recovering electric power by 270kw in an average hour;
reducing turbine installed power by 700kw, and recovering electric power by 400kw in an average hour;
reducing turbine installed power by 1200kw, and recovering electric power by 620kw in an average hour;
the installed power of the forward-bleed turbine is 4000kw, and the average recovery power is 2000kw in an hour;
the total recovery rate is 3660kwh/h, and the effective energy recovery rate is 75%;
example 3
Coal hydrogen production shift gas amount 300000Nm3/h, pressure 3.6MPa (g), temperature 40 ℃, CO 2 Content 43%, H 2 55% CO content, 1.0% N 2 Content 1.0%, CH 4 The content is 1 percent; the hydrogen, CO2 and low heating value gas components of the product are shown in the following table.
The PSA pressure swing adsorption separation process of the invention is adopted for separation by an effective recovery method.
Product H 2 Purity is more than or equal to 98%, CO 2 Less than or equal to 1 percent and is used for synthesizing related products, wherein CO+N 2 +CH 4 The average value is less than or equal to 1 percent;
reverse put into CO 2 The purity of the product gas is more than or equal to 98 percent, and the product gas is used for synthesizing related products, wherein CO+H 2 +CH 4 The average value is less than or equal to 1 percent;
flushing gas as low-heat value fuel gas, CO 2 The content is more than or equal to 86 percent, wherein CO+H 2 +CH 4 Average 10.52%;
hydrogen product yield 98%, wherein CO 2 Less than or equal to 1 percent. The pressure of the methane product is 0.12MPa (A), and the pressure of the hydrogen product is more than or equal to 3.5MPa. The PSA pressure swing adsorption process adopts two sets of air flow energy recovery Turbines (TP) with inner diameters of 3.6 meters and 10 < -2 > -5/P processes connected in parallel, the total adsorption resistance drop is less than or equal to 0.05MPa, and an air flow energy recovery Turbine (TP) is installed on a main pipe with 5 times of pressure equalizing and 1 time of forward discharging and reverse dischargingA heater (JRQ) is additionally arranged at an inlet of an air flow energy recovery Turbine (TP), and the air flow is heated by utilizing low-position waste heat in a CO conversion process so as to improve the energy recovery rate; and meanwhile, the temperature is prevented from being too low in winter, and the lower part of the adsorption tower bed layer is prevented from being frozen. The generator adopts a motor generator, and the voltage equalizing later stage is appropriately powered up to shorten the regeneration time.
Firstly, the turbine installed power is reduced by 500kw, and the electric power is recovered by 380kw in an average time;
reducing turbine installed power by 600kw and recovering electric power by 450kw in an average hour;
thirdly, the turbine installed power is reduced by 750kw, and the average recovery power is 600kw in an hour;
reducing turbine installed power by 1000kw, and recovering electric power by 850kw in an average hour;
reducing turbine installed power 1800kw, and recovering electric power 1400kw in an average time;
the installed power of the forward air discharge and reverse air discharge turbine is 6000kw, and the average recovery power is 4500kw in an hour;
the total recovery rate is that the electric power is 8180kwh/h and the effective energy recovery rate is 67%.
The above examples are given by way of illustration only and are not intended to be limiting. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary or impossible to cite all the embodiments here, and obvious variations or modifications are still included from this list, which are within the scope of protection of the invention.
Claims (10)
- An effective recovery method in a PSA pressure swing adsorption separation process, characterized by: in the effective gas recovery and additive regeneration process in an adsorption tower of a PSA pressure swing adsorption separation process, arranging a gas flow energy conversion device (TP) in a channel for discharging gas from the adsorption tower and the container with relatively high pressure to the adsorption tower and the container with relatively low pressure, converting the energy of the gas flow from the adsorption tower and the container with relatively high pressure into mechanical energy, and converting the mechanical energy into electric energy through a connected generator (FD);a heater (JRQ) is arranged in an air inlet pipeline of the airflow energy conversion device (TP) so as to heat the airflow and increase the effective energy obtaining amount of the airflow;the low-temperature gas expanded by the airflow energy conversion device (TP) is used for working, the bed temperature of the other adsorption tower is reduced, the adsorption capacity is improved, the volume of the adsorbent is reduced, and the temperature of a separated product is reduced;feeding cold energy back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ) by using low-temperature high-pressure product Gas (GYCPQ), and reducing the bed temperature of the adsorption tower and the low-temperature low-pressure product gas (DYCPQ) to lower temperature;similarly, the low-pressure product gas with low temperature is fed back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ), so that the bed temperature of the adsorption tower and the high-pressure product Gas (GYCPQ) are reduced to lower temperature;the low-temperature high-pressure product Gas (GYCPQ) and the low-temperature low-pressure product gas (DYCPQ) are fed back to the dehydration raw material gas (TSYLQ) through a cold exchanger (LJHQ), so that the temperature of the adsorption tower bed layer is reduced, and simultaneously, the pressure of the pressure swing adsorption process, the pressurizing energy consumption of the raw material gas and the CO produced by energy sources are reduced 2 Discharging;in the pressure swing adsorption process provided with a plurality of airflow energy conversion devices (TP), the cold energy of the outlet air of each airflow energy conversion device (TP) is concentrated and output to a cooling device by adopting a circulating cold-conducting liquid serial cold exchange circulation mode;the cold obtained by the pressure swing adsorption process provided with the airflow energy conversion device (TP) is exchanged to another set of pressure swing adsorption process device or ammonia cooling device or other devices such as air cryogenic separation devices requiring low temperature through dividing wall heat exchange or liquid circulation mode, so that the process temperature can be reduced.
- 2. The method according to claim 1, wherein the adsorption columns (a) to (H) in the same cycle are all sequentially passed through a common drop header (1 JJZG) and then flowed into a common drop energy conversion device (TP 1) and then sequentially passed through a common riser (1 JSZG) and then flowed into the corresponding adsorption column.The two uniform descending air flows from the adsorption tower (A) to the adsorption tower (H) in the same circulation flow into the two uniform descending air flow energy conversion device (TP 2) after passing through the two uniform descending main pipes (2 JJZG) in order, and flow into the corresponding adsorption towers after passing through the two uniform ascending main pipes (2 JJZG) in order;the three-average descending air flows from the adsorption tower (A) to the adsorption tower (H) in the same circulation flow into the three-average descending air flow energy conversion device (TP 3) after passing through the three-average descending main pipe (3 JJZG) in order, and flow into the corresponding adsorption tower after passing through the three-average ascending main pipe (3 JJZG) in order;when the system pressure is high, the pressure equalizing times will exceed 3 times, namely the N-th uniform pressure drop air flow of the adsorption towers in the same cycle passes through the N-th uniform descending main pipe in sequence, then flows into the N-th uniform descending air flow energy conversion device, and flows into the corresponding adsorption towers after passing through the N-th uniform ascending main pipe in sequence, wherein the number of the adsorption towers in the same cycle is less than or equal to 50.
- 3. The method for recovering energy in PSA pressure swing adsorption separation according to claim 1, wherein the energy conversion device (TP) for gas flow directly disposed at the inlet and outlet pipes at the top of the adsorption column converts the energy of gas flow flowing into the adsorption column into mechanical energy and the energy of gas flow flowing out of the adsorption column into mechanical energy;the airflow energy conversion device (TP) arranged on the inlet and outlet pipelines at the top of the adsorption tower is provided with a bypass one-way valve, only the energy of the airflow entering the tower can be converted into mechanical energy, and the airflow exiting the tower does not flow out of the adsorption tower through the airflow energy conversion device (TP).
- 4. The method for recovering efficiency in PSA pressure swing adsorption separation according to claim 1, wherein the generator (FD) connected to the gas flow energy conversion device (TP) is changed into a motor generator, and electric energy can be input to drive the gas flow energy conversion device (TP) at the later stage of the pressure equalization period, so as to increase the gas flow speed, shorten the pressure equalization time, and further shorten the pressure swing adsorption cycle.
- 5. The method for recovering efficiency in PSA pressure swing adsorption separation according to claim 1, wherein the rotating impellers of the air flow energy conversion devices (TP) arranged in the one pressure equalizing main pipe (1 JYZG), the two pressure equalizing main pipes (2 JYZG), the three pressure equalizing main pipes (3 JYZG), the N times pressure equalizing main pipes (NLYZG) and the forward main pipe (SFZG) rotate in one direction, and air flows at both ends of the air flow energy conversion devices (TP) enter in the direction of rotation of the impellers to transfer energy to the impellers to be converted into mechanical energy;the bleed air flows of the adsorption tower (A, B, C, D) and the adsorption tower (E, F, G, H) at the two ends of the air flow energy conversion device (TP) are respectively and sequentially sent to the adsorption tower at the other end through the air flow energy conversion device (TP) by program control; the number of the adsorption towers is less than or equal to 50; n in the N times equalizing manifold (nJYzg) includes the forward manifold: an integer of 1.ltoreq.N.ltoreq.16.
- 6. The method for efficient recovery in a PSA pressure swing adsorption separation process according to claim 1, wherein the control of the adsorption column bed temperature is achieved by adjustment of heater (JRQ) temperature and adjustment of energy conversion efficiency of the gas stream energy conversion device (TP).
- 7. The method for recovering efficiency in PSA pressure swing adsorption separation according to claim 1, wherein the turbine wheel is rotated in one direction by controlling the positions of check valves installed at the inlet and outlet of the air flow energy conversion device (TP) so that the air flow energy conversion device (TP) is rotated to intake air along the impeller when the two ends are alternately intake air; and the impeller shaft and the flywheel are used for storing energy by inertia, so that the electric power amplitude caused by air flow pressure difference and flow change is reduced.
- 8. The method for recovering energy in PSA pressure swing adsorption separation process according to claim 1, wherein the energy recovery is performed by installing a gas stream energy conversion device (TP) in the bottom equalizing main (tdJYzg) and in the reverse bleed main (NFQZG) of the adsorption tower.
- 9. The method for recovering energy in PSA pressure swing adsorption separation process according to claim 1, wherein the energy recovery by the gas stream energy conversion device (TP) is performed in the same circulation flow, in the pressure equalizing line of the adsorption tower top, in the pressure equalizing line of the adsorption tower bottom, in the exhaust gas line of the adsorption tower bottom, in the final pressure boosting main pipe of the adsorption tower top.
- 10. The method for recovering efficiency in a PSA pressure swing adsorption separation process according to claim 1, wherein a gas stream energy conversion device (TP) and a heater (JRQ) are installed in the pressure equalization line of the temperature swing adsorption separation process to recover efficiency in the purge gas and control the temperature of the temperature swing adsorption bed.
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