CN115651705A - Membrane separation hydrogen extraction system and method for low-carbon hydrocarbon entering working section - Google Patents
Membrane separation hydrogen extraction system and method for low-carbon hydrocarbon entering working section Download PDFInfo
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- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a membrane separation hydrogen extraction system and method for a low-carbon hydrocarbon entering working section, belonging to the technical field of chemical gas separation 2 The flash evaporation gas mixed gas of S is cooled and separated, then the gas entering the coalescence filter is heated by a heater, the temperature of the gas entering a membrane is far away from the dew point, then the gas enters a membrane separator for selective separation, the permeation gas is extracted, and finally the pressure is increased by a permeation gas compressor to obtain the qualified permeation gas, so that the technical problem that the Fischer-Tropsch synthesis tail gas purge quantity demand is not matched with the existing device is solved, the hydrogen recovery rate is improved, the unit consumption of the Fischer-Tropsch synthesis fresh gas is reduced, and the Fischer-Tropsch synthesis fresh gas is excellentThe operating conditions of the molecular sieve and the expansion machine are changed, and the long-period stable operation of the low-carbon hydrocarbon recovery system is ensured. Meanwhile, the content of hydrogen in the tail gas can be reduced to 54%, the recovery rate of the low-carbon hydrocarbon recovery device is improved, and the maximum operation benefit of enterprises is realized.
Description
Technical Field
The invention belongs to the technical field of chemical gas separation, and particularly relates to a membrane separation hydrogen extraction system and method for a low-carbon hydrocarbon entering working section.
Background
The low-carbon hydrocarbon recovery device adopts a gas cryogenic separation technology, the core of the cryogenic separation is an expansion compressor, and the raw material gas mainly comprises hydrogen, carbon monoxide, carbon dioxide, argon, nitrogen, methane, C2, C3 and C4+. And (3) after the tail gas of the Fischer-Tropsch synthesis system is subjected to secondary decarburization, the tail gas enters a low-carbon hydrocarbon recovery system to be used as a raw material gas, after cryogenic separation, the gas phase is sent to a PSA hydrogen recovery device to extract hydrogen with the purity of 99.5%, the hydrogen is sent to a hydrogenation device, and liquid hydrocarbons are sent to an oil product refining section to be subjected to deep processing to obtain a qualified oil product.
In the process of preparing the oil from the coal by adopting the Fischer-Tropsch synthesis process, the problem of two-stage differentiation of the original design value and the actual value of the Fischer-Tropsch synthesis tail gas components can be solved, and the problem is changed from low hydrogen to high hydrogen, so that the technical problem that the Fischer-Tropsch synthesis tail gas emission demand is not matched with the existing low-carbon hydrocarbon recovery device (namely a tail gas treatment device), which is a main factor for restricting the operation and adjustment of a Fischer-Tropsch synthesis system. The hydrogen content in the raw material gas of the low-carbon hydrocarbon recovery system reaches 62-67%, the raw material gas is seriously deviated from the design working condition, and the service life of the expansion compressor is shortened; and the excessive ineffective gas in the raw material gas causes the reduction of C3+ partial pressure and the reduction of the recovery rate of the low-carbon hydrocarbon liquid product. The redundant gas can only be sent to the fuel gas pipe network for burning, which causes the waste of energy and is not economical in operation. Meanwhile, due to the gas-liquid entrainment phenomenon of the low-carbon hydrocarbon feed gas, the molecular sieve in the dehydrator is easy to pulverize, the service life is shortened, the dehydration performance is rapidly reduced, the molecular sieve needs to be replaced periodically, and the production cost is increased. The content of hydrogen in flash steam of an oil product refining device is up to more than 70 percent, and the flash steam is merged into a byproduct fuel gas pipe network to be used as fuel gas at present, thereby causing resource waste. The hydrogen is used as effective gas for Fischer-Tropsch synthesis reaction, and the effective separation and recovery of the hydrogen are problems which need to be continuously explored in the domestic gas separation technology.
Disclosure of Invention
In order to solve the defects of the prior art, the invention aims to provide a low-carbon hydrocarbon entering working section membrane separation hydrogen extraction system and a low-carbon hydrocarbon entering working section membrane separation hydrogen extraction method.
In order to realize the purpose, the technical scheme of the invention is as follows:
in one aspect, a membrane separation hydrogen extraction system for a low-carbon hydrocarbon inlet section comprises:
the flash evaporation gas pretreatment system is used for carrying out desulfurization treatment on flash evaporation gas and comprises an adsorption tank;
the multistage separation system is used for cooling and separating the mixed gas and removing heavy hydrocarbon and moisture in the mixed gas, and comprises a first heat exchanger, a raw material gas separator, a cooler and a membrane separation skid-mounted inlet separator; the first heat exchanger heat medium inlet is connected with the decarbonization two-section tail gas outlet and the flash gas outlet of the flash gas pretreatment system, the first heat exchanger heat medium outlet is connected with the feed inlet of the raw material gas separator, the gas phase of the raw material gas separator is connected with the membrane separation skid-mounted inlet separator through the cooler, and the liquid phase of the raw material gas separator is merged into the liquid phase pipeline of the decarbonization oil-water separator; the gas phase of the membrane separation skid-mounted inlet separator enters a next treatment system, and the liquid phase is merged into a liquid phase pipeline of the decarbonization oil-water separator;
the membrane separation system is used for selectively separating the mixed gas and comprises a filter, a heater and a membrane separator; and a gas phase inlet of the filter is connected with a gas phase outlet of the membrane separation skid-mounted inlet separator, the filtered gas phase sequentially passes through the first heat exchanger and the heater and then enters the membrane separator, after separation, the residual gas is conveyed to the low-carbon hydrocarbon recovery device, and the permeate gas is conveyed to the permeate gas compression system.
On the other hand, a method for extracting hydrogen by membrane separation of a low-carbon hydrocarbon entering working section adopts the system for extracting hydrogen by membrane separation of the low-carbon hydrocarbon entering working section;
the method specifically comprises the following steps: the method comprises the following steps of conveying flash steam together with decarbonized two-stage tail gas to a first heat exchanger after desulfurization through an adsorption tank, cooling to 28-30 ℃, then conveying the flash steam into a raw material gas separator, merging a separated liquid phase into a liquid phase pipeline of a decarbonized oil-water separator, conveying the separated liquid phase into a liquid phase pipeline of the decarbonized oil-water separator, cooling the separated gas phase into a cooler to 8-12 ℃, conveying the cooled gas phase into a membrane separation skid-mounted inlet separator, conveying the separated gas phase into a filter for filtration and separation, merging the filtered liquid phase into a liquid phase pipeline of the decarbonized oil-water separator, conveying the filtered gas phase serving as a cooling medium of the first heat exchanger through a heater after heat exchange to enable the temperature of a gas entering a membrane to be far away from a dew point, conveying the gas to the membrane separator, selectively separating heated mixed gas, conveying the permeated gas into a low-carbon hydrocarbon recovery device, conveying the permeated gas into a permeated gas compression system, and compressing and pressurizing to obtain qualified permeated gas and conveying the purified gas pipe network.
The beneficial effects of the invention are as follows:
1. according to the membrane separation hydrogen extraction system for the low-carbon hydrocarbon entering section, disclosed by the invention, before the low-carbon hydrocarbon recovery device is arranged, the flash evaporation gas and the decarbonized two-section tail gas are treated, so that the problems that the low-carbon hydrocarbon recovery is influenced by too high hydrogen content, too much invalid gas and gas-liquid entrainment in the low-carbon hydrocarbon feed gas are avoided, and the technical problem that the emission requirement of Fischer-Tropsch synthesis tail gas is not matched with the conventional low-carbon hydrocarbon recovery device is successfully solved.
2. The low-carbon hydrocarbon entering working section membrane separation hydrogen extraction system disclosed by the invention is used for treating the flash evaporation gas and the decarbonized two-section tail gas, effectively separating and recovering hydrogen, avoiding resource waste and increasing benefits for enterprises.
3. The low-carbon hydrocarbon entering working section membrane separation hydrogen extraction system improves the operation condition of the expansion compressor, increases the refrigeration effect of the compressor, enables the compressor to meet the refrigeration requirement of the system, simultaneously realizes the long-period stable operation requirement of the molecular sieve of the dehydrator of the low-carbon hydrocarbon system, and reduces the production cost for enterprises.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are included to illustrate an exemplary embodiment of the invention and not to limit the invention.
FIG. 1 is a schematic diagram showing the structure of a membrane separation hydrogen-extracting system of a low-carbon hydrocarbon inlet section in example 1 of the present invention, in which only one coalescing filter is provided, and the remaining spare coalescing filters are not shown; because each group of membrane separator group consists of 4 membrane separators and the connection mode is the same, only one group of membrane separator group is drawn, and the rest 7 groups are omitted and not drawn.
Wherein, the first adsorption tank: 101, second canister: 102, a first heat exchanger: 201, raw material gas separator: 202, propylene chiller: 203, membrane separation skid-mounted inlet separator: 204, coalescing filter: 301, heater: 302, membrane separator: 303, permeate gas cooler: 304, permeate gas compressor: 305, retentate cooler: 306, loop cooler: 307.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
In view of the technical problem that the current Fischer-Tropsch synthesis tail gas emission demand is not matched with the existing low-carbon hydrocarbon recovery device and the problem of a large amount of hydrogen in Fischer-Tropsch synthesis tail gas and flash steam, the invention provides a low-carbon hydrocarbon entering section membrane separation hydrogen extraction system and method.
In a typical embodiment of the present invention, a membrane separation hydrogen-extracting system for a low-carbon hydrocarbon entering section includes:
the flash evaporation gas pretreatment system is used for carrying out desulfurization treatment on flash evaporation gas and comprises an adsorption tank;
the multistage separation system is used for cooling and separating the mixed gas and removing heavy hydrocarbon and moisture in the mixed gas, and comprises a first heat exchanger, a raw material gas separator, a cooler and a membrane separation skid-mounted inlet separator; a first heat exchanger heat medium inlet is connected with a decarbonization two-section tail gas outlet and a flash gas outlet of the flash gas pretreatment system, the first heat exchanger heat medium outlet is connected with a feed inlet of a raw material gas separator, a gas phase of the raw material gas separator is connected with a membrane separation skid-mounted inlet separator through a cooler, and a liquid phase of the raw material gas separator is merged into a liquid phase pipeline of a decarbonization oil-water separator; the gas phase of the membrane separation skid-mounted inlet separator enters a next treatment system, and the liquid phase is merged into a liquid phase pipeline of the decarbonization oil-water separator;
the membrane separation system is used for selectively separating the mixed gas and comprises a filter, a heater and a membrane separator; and a gas phase inlet of the filter is connected with a gas phase outlet of the membrane separation skid-mounted inlet separator, the filtered gas phase sequentially passes through the first heat exchanger and the heater and then enters the membrane separator, after separation, the residual gas is conveyed to the low-carbon hydrocarbon recovery device, and the permeate gas is conveyed to the permeate gas compression system.
In some implementations of this embodiment, the adsorption tank is one or more adsorption tanks connected in parallel.
In some implementations of this embodiment, the canister uses zinc oxide as the adsorbent. H 2 The S and the ZnO are subjected to acid-base neutralization reaction, so that the content of hydrogen sulfide in flash steam is less than or equal to 1ppm
The multistage separation system comprises a first heat exchanger, a raw material gas separator, a cooler and a membrane separation skid-mounted inlet separator, wherein the mixed gas is cooled and separated by a method of removing heavy hydrocarbon and moisture in the heat condensed mixed gas by using a coolant, gas-liquid entrainment is effectively eliminated, the working conditions of entering a membrane and a molecular sieve gas are improved, the service life of a membrane core of the membrane separator is prolonged, and the pulverization of the molecular sieve is reduced. Preferably, the cooler is a propylene cooler.
In some implementations of this embodiment, the filter is a coalescing filter.
In some embodiments of this embodiment, the filter is one or more filters connected in parallel, and only one of the filters is used when the membrane separation hydrogen extraction system of the low-carbon hydrocarbon inlet section is in operation, and the rest of the filters are spare. A plurality of (more than or equal to 2) coalescence type filters are arranged as a first-stage filtering system for gas-liquid filtering and separating, so that liquid phase in gas can be fully removed, gas-liquid entrainment is avoided, the molecular sieve pulverization phenomenon in the low-carbon hydrocarbon recovery device is reduced, and meanwhile, if a filter element is replaced by the filter or a fault condition and the like occur, other filters can be switched to use, and the system is prevented from being stopped.
In some embodiments of this example, the membrane separators are multiple groups of membrane separators, preferably ≧ 8 groups of 4 stations per group, as the gas separation system. The membrane separator adopts a method of combining different solubility, diffusion coefficient and permeation rate of various gases in the membrane to realize the separation of the gases.
Preferably, the membrane separators are connected in parallel, and the membrane separators can be cut out independently. The multi-group membrane separators are connected in parallel to remove H from the decarbonized two-section tail gas through the adsorption tank 2 And selectively separating the mixed gas of the flash evaporation gas of S.
Preferably, the membrane separator is provided with ultra-warm and cryogenic interlocks and a one-key shut down system is designed in the control room. Because the temperature of the process gas is too low, the process gas is easy to carry liquid, so that the membrane is adhered by hydrocarbon substances, membrane filaments are possibly dissolved and broken, and the separation performance of the membrane is influenced; when the temperature is too high and exceeds the tolerance temperature of the membrane, the molecular structure of the membrane is changed by the too high temperature, and the performance of the membrane is influenced. Therefore, the membrane separator is provided with ultra-temperature and low-temperature interlocking, and a one-key parking system is designed in a control room to protect the safe and stable operation of the membrane.
In some embodiments of this embodiment, the permeate gas compression system includes a permeate gas compressor configured to compress the permeate gas and deliver the pressurized permeate gas to a purification pipeline network.
Preferably, the permeate gas compressor is a reciprocating compressor, and the permeate gas (hydrogen) is pressurized by adopting a multi-stage compression method of expansion, suction, compression and exhaust.
Preferably, the permeate gas compression system further comprises a loop cooler through which the pressurized permeate gas is partially sent to the PSA hydrogen recovery unit. The pressurized permeating gas conveyed to the PSA hydrogen recovery device replaces feed gas to enter PSA to replace purified gas to reduce and supply hydrogen for oil products and catalysts in a low-carbon hydrocarbon parking state.
In some implementations of this embodiment, the membrane separation system further includes a permeate gas cooler, a retentate gas cooler.
The permeating gas obtained by the separation of the membrane separator enters a permeating gas compression system after passing through a permeating gas cooler;
and the residual gas obtained by the separation of the membrane separator enters a low-carbon hydrocarbon recovery device after passing through a residual gas cooler.
In some embodiments of this embodiment, the retentate gas is connected to the low pressure fuel gas grid pipe by a pipe. And (4) residual gas is used as supplementary gas of the low-pressure fuel gas pipe network, and the low-pressure fuel gas pipe network is maintained to normally operate in a low-carbon hydrocarbon shutdown state.
In some embodiments of this embodiment, the low-pressure fuel gas pipe network is connected to the gas holder pipeline through a pipeline, and the surplus gas is used as a medium-pressure fuel gas pipe network make-up gas to maintain the normal operation of the thermoelectric combustion engine in a low-carbon hydrocarbon shutdown state.
In another exemplary embodiment of the present invention, the method for extracting hydrogen by membrane separation in a low-carbon hydrocarbon feeding section adopts the system for extracting hydrogen by membrane separation in a low-carbon hydrocarbon feeding section described in the first exemplary embodiment.
The membrane separation hydrogen extraction method for the low-carbon hydrocarbon entering working section specifically comprises the following steps: the flash evaporation gas is desulfurized through an adsorption tank and then is conveyed to a first heat exchanger together with the decarbonization two-stage tail gas to be cooled to 28-30 ℃, and preferably 30 ℃; then the raw material gas enters a raw material gas separator, the separated liquid phase is merged into a liquid phase pipeline of a decarbonization oil-water separator, the separated gas phase enters a cooler to be cooled to 8-12 ℃ (preferably 10 ℃), then the gas phase enters a membrane separation skid-mounted inlet separator, the separated liquid phase is merged into a liquid phase pipeline of the decarbonization oil-water separator, the separated gas phase is conveyed to a coalescing filter to be filtered and separated, the filtered liquid phase is merged into the liquid phase pipeline of the decarbonization oil-water separator, the filtered gas phase is used as a cold medium of a first heat exchanger, the cold medium is subjected to heat exchange and then passes through a heater, the temperature of the inlet membrane is far away from the dew point and then conveyed into the membrane separator, the heated mixed gas is subjected to selective separation, the residual gas enters a low-carbon hydrocarbon recovery device, the permeate gas enters a permeate gas compression system, and is subjected to multistage compression and pressure increase to obtain qualified permeate gas and then the permeate gas is conveyed to a purified gas pipe network.
In some examples of this embodiment, the flash gas pretreatment system utilizes an adsorption tank to desulfurize the flash gas and a chemisorption process using zinc oxide as the adsorbent. The working principle of flash evaporation gas desulfurization is as follows: znO + H 2 S＝ZnS+H 2 O, the reaction mechanism is simple and cannot be regenerated. Flash steam processTwo zinc oxide adsorption tanks in the oil refining device are used for desulfurization, H 2 And (3) carrying out acid-base neutralization reaction on the S and ZnO to ensure that the flash steam meets the qualified requirement (the content of hydrogen sulfide in the flash steam is less than or equal to 1 ppm) and is used as a feed gas of the membrane separation hydrogen extraction device.
In some examples of this embodiment, two coalescing filters may be operated in parallel in a coalescing separation process to achieve maximum operating efficiency; the single operation can be carried out according to the actual situation.
In some examples of this embodiment, the heater is heated with 0.6MPa steam to heat the gas phase to 60-70 ℃ and then enters the membrane separator.
In some embodiments of this embodiment, the permeate gas is cooled to 40 ℃ by the permeate gas cooler and then sent to the compressor for pressurization, and the permeate gas is pressurized to 3.4Mpa and sent to the purified gas pipe network, or the pressurized permeate gas is sent to the feed gas pipeline of the PSA hydrogen recovery unit by the reflux cooler.
In order to make the technical solutions of the present invention more clearly understood by those skilled in the art, the technical solutions of the present invention will be described in detail below with reference to specific embodiments.
The following examples separate permeate gas (hydrogen) and retentate gas (tail gas) using a pleisen membrane, which is commercially available.
Example 1
As shown in fig. 1, the membrane separation hydrogen extraction system (provided with 8 membrane separator sets, since each membrane separator set is composed of 4 membrane separators and connected in the same manner, only one membrane separator set is shown in fig. 1, and the remaining 7 membrane separator sets are omitted and not shown) of the low carbon hydrocarbon inlet section comprises: a first adsorption tank 101, a second adsorption tank 102, a first heat exchanger 201, a feed gas separator 202, a propylene cooler 203, a membrane separation skid inlet separator 204, a coalescing filter 301, a heater 302, a membrane separator 303, a permeate gas cooler 304, a permeate gas compressor 305, a retentate gas cooler 306, a loop cooler 307.
A feed gas inlet of the first heat exchanger 201 is connected with a tail gas outlet of the decarburization second section and flash gas outlets of the first adsorption tank 101 and the second adsorption tank 102, a heat medium outlet of the first heat exchanger 201 is connected with a feed inlet of a raw material gas separator 202, a gas phase of the raw material gas separator 202 is connected with a membrane separation skid-mounted inlet separator 204 through a propylene cooler 203, and a liquid phase of the raw material gas separator 202 is merged into a liquid phase pipeline of the decarburization oil-water separator; the gas phase of the membrane separation skid-mounted inlet separator 204 enters the coalescing filter 301, and the liquid phase is merged into a liquid phase pipeline of the decarbonization oil-water separator; after the mixed gas is filtered by a coalescing filter 301, a gas phase sequentially passes through a first heat exchanger 201 and a heater 302 and then enters a membrane separator 303, after separation, the residual gas is conveyed to a low-carbon hydrocarbon recovery device, the permeation gas separated by the membrane separator 303 sequentially passes through a permeation gas cooler 304 and a permeation gas compressor 305, the permeation gas is pressurized, and the pressurized permeation gas is conveyed to a purified gas pipe network; the pressurized permeate gas can be controlled by a valve to pass through a loop cooler 307 and be conveyed to a PSA hydrogen recovery device; the liquid phase of coalescing filter 301 merges into the decarbonized oil-water separator liquid line.
The permeation gas compressor adopts a reciprocating compressor, and the permeation gas (hydrogen with the purity of 94-96 percent and the pressure of 0.5 MPa) is pressurized to 3.4MPa and sent to a purification gas pipe network through the multi-stage compression mode of expansion, suction, compression and exhaust. Because the single-stage compressor can not pressurize the permeate gas to 3.4Mpa, the three-stage compressor is selected to compress and pressurize the permeate gas in consideration of the cost of the compressor and the energy-saving problem.
The volume of a single zinc oxide adsorption tank is 5.9m 3 The flash evaporation gas is desulfurized through two zinc oxide adsorption tanks in the oil product refining device, and H 2 And carrying out acid-base neutralization reaction on the S and the ZnO to ensure that the content of hydrogen sulfide in the flash steam is less than or equal to 1ppm.
The first heat exchanger 201 is a single shell pass fixed tube plate heat exchanger (BEM) with a heat exchange area of 477.6m 2 The number/specification of the heat exchange tubes is as follows: 1860/phi 19x2mm, the length of the straight section is 4500mm. The propylene cooler 203 is an integral seal head kettle type U-shaped tubular heat exchanger (BKU), and the heat exchange area is 68m 2 The number/specification of the heat exchange tubes is as follows: 149U/phi 25x2.5mm, and the length of the straight section is 3000mm. The temperature is reduced through the first heat exchanger 201 and the propylene cooler 202, so that the heavy hydrocarbon in the feed gas is cooled. First heat exchanger 201, using propylene cooler 203, the cooled cold process medium exchanges heat with the feed gas, so that the cold energy is reasonably utilized.
The temperature of the membrane is far away from the saturated dew point of the gas phase through the heater 302, hydrogen rapidly permeates through the membrane filaments and is gathered in the membrane through the selectivity of the polyimide membrane, and the purity of the hydrogen of the permeated gas can reach more than 94%.
The membrane separators 303 are 8 sets of membrane separators, 4 membrane separators per set. The 8 groups of membrane separators are connected in parallel by adopting a plurality of groups of membrane separators, the single group of membrane separators can be connected in a mode of independent switching, the 8 groups of membrane separators are all provided with over-temperature and low-temperature interlocking, and a one-key parking system is designed in a control room.
Example 2
The method for extracting hydrogen by membrane separation of low-carbon hydrocarbon entering a workshop section adopts the system for extracting hydrogen by membrane separation of low-carbon hydrocarbon entering the workshop section in the example 1.
The method specifically comprises the following steps: conveying the flash steam together with decarbonized two-stage tail gas after desulfurization through an adsorption tank to a first heat exchanger to cool to 30 ℃, then conveying the flash steam into a raw material gas separator, introducing the separated liquid phase into a liquid phase pipeline of a decarbonized oil-water separator, introducing the separated gas phase into a cooler to cool to 10 ℃, then conveying the separated gas phase into a membrane separation skid-mounted inlet separator, introducing the separated liquid phase into a liquid phase pipeline of the decarbonized oil-water separator, conveying the separated gas phase to a coalescing filter to carry out filtration and separation, introducing the filtered liquid phase into a liquid phase pipeline of the decarbonized oil-water separator, taking the filtered gas phase as a cooling medium of the first heat exchanger, carrying out heat exchange, then passing through a heater, heating to 60-70 ℃, then conveying into a membrane separator group, carrying out selective separation on the heated mixed gas, and carrying out residual gas (1.5MPa, 7.5 ten thousand Nm & ltm & gtm & gton) after passing through the membrane separator group 3 H) entering a low-carbon hydrocarbon recovery device after passing through a residual gas cooler; extract 2.5 ten thousand Nm 3 The permeable gas (hydrogen) with the purity of more than or equal to 94 percent and the pressure of 0.5MPa is cooled to 40 ℃ by a permeable gas cooler and then is sent to a permeable gas compressor, the permeable gas compressor raises the pressure of the permeable gas to 3.4MPa and then sends the permeable gas to a purified gas pipe network, or the pressurized permeable gas is sent to a raw gas pipeline of a PSA hydrogen recovery device by a reflux cooler.
By adopting the system and the method of the invention, the synthesis system is improvedEffective gas (H) 2 ) The recovery rate is reduced, the unit consumption of fresh gas for Fischer-Tropsch synthesis is reduced, the working condition of low-carbon hydrocarbon gas intake is improved, the operating conditions of a molecular sieve and an expansion machine are optimized, and the long-period stable operation of a low-carbon hydrocarbon recovery system is ensured. The extraction and concentration reduction of the membrane separation device realize the improvement of the whole load of the tail gas treatment device, recover the liquid product in the vent gas and improve the yield. Meanwhile, the hydrogen content in the tail gas can be reduced to 54%, the recovery rate of the low-carbon hydrocarbon recovery device is improved, the surplus hydrogen is recycled, and the maximum operation benefit of enterprises is realized.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The membrane separation hydrogen-extracting system for the low-carbon hydrocarbon entering working section is characterized by comprising:
the flash evaporation gas pretreatment system is used for carrying out desulfurization treatment on flash evaporation gas and comprises an adsorption tank;
the multistage separation system is used for cooling and separating the mixed gas and removing heavy hydrocarbon and moisture in the mixed gas, and comprises a first heat exchanger, a raw material gas separator, a cooler and a membrane separation skid-mounted inlet separator; a first heat exchanger heat medium inlet is connected with a decarbonization two-section tail gas outlet and a flash gas outlet of the flash gas pretreatment system, the first heat exchanger heat medium outlet is connected with a feed inlet of a raw material gas separator, a gas phase of the raw material gas separator is connected with a membrane separation skid-mounted inlet separator through a cooler, and a liquid phase of the raw material gas separator is merged into a liquid phase pipeline of a decarbonization oil-water separator; the gas phase of the membrane separation skid-mounted inlet separator enters a next treatment system, and the liquid phase is merged into a liquid phase pipeline of the decarbonization oil-water separator;
the membrane separation system is used for selectively separating the mixed gas and comprises a filter, a heater and a membrane separator; and a gas phase inlet of the filter is connected with a gas phase outlet of the membrane separation skid-mounted inlet separator, the filtered gas phase sequentially passes through the first heat exchanger and the heater and then enters the membrane separator, after separation, the residual gas is conveyed to the low-carbon hydrocarbon recovery device, and the permeate gas is conveyed to the permeate gas compression system.
2. The membrane separation hydrogen extraction system of a low-carbon hydrocarbon inlet workshop section according to claim 1, wherein the adsorption tank is one or more adsorption tanks connected in parallel;
or, the adsorption tank adopts zinc oxide as an adsorbent.
3. The low hydrocarbon inlet section membrane separation hydrogen extraction system of claim 1, wherein the filter is a coalescing filter;
or one or more filters connected in parallel are adopted, when the low-carbon hydrocarbon entering workshop section membrane separation hydrogen extraction system works, only one filter is suitable, and the rest filters are reserved.
4. The membrane separation hydrogen extraction system of the low-carbon hydrocarbon inlet working section according to claim 1, wherein the membrane separators are a plurality of groups of membrane separators, preferably more than or equal to 8 groups, and each group comprises 4 membrane separators;
further preferably, the multiple groups of membrane separators are connected in parallel, and the single group of membrane separators can be connected in an independent cutting mode.
5. The membrane separation hydrogen extraction system of a low carbon hydrocarbon inlet section according to claim 1, wherein the membrane separator is provided with ultra-high temperature and low temperature interlocking, and a one-key shutdown system is designed in a control room.
6. The membrane separation hydrogen extraction system of a low carbon hydrocarbon inlet section according to claim 1, wherein the permeate gas compression system comprises a permeate gas compressor for compressing the permeate gas and delivering the pressurized permeate gas to a purification pipe network;
preferably, the permeate gas compressor is a reciprocating compressor;
preferably, the permeate gas compression system further comprises a loop cooler through which the pressurized permeate gas is partially sent to the PSA hydrogen recovery unit.
7. The low carbon hydrocarbon inlet section membrane separation hydrogen extraction system of claim 1, wherein the membrane separation system further comprises a permeate cooler, a retentate cooler;
the permeation gas obtained by the separation of the membrane separator enters a permeation gas compression system after passing through a permeation gas cooler;
the residual gas separated by the membrane separator enters a low-carbon hydrocarbon recovery device after passing through a residual gas cooler;
or the residual gas is connected with the low-pressure fuel gas pipe network pipeline through a pipeline.
8. The method for extracting hydrogen by membrane separation at a low-carbon hydrocarbon feeding section is characterized in that a low-carbon hydrocarbon feeding section membrane separation hydrogen extraction system according to any one of claims 1 to 7 is adopted;
the method specifically comprises the following steps: the method comprises the steps that flash evaporation gas is desulfurized through an adsorption tank and then is conveyed to a first heat exchanger together with decarbonized two-section tail gas to be cooled to 28-30 ℃, then the flash evaporation gas enters a raw material gas separator, a separated liquid phase is merged into a liquid phase pipeline of a decarbonized oil-water separator, a separated gas phase enters a cooler to be cooled to 8-12 ℃, then enters a membrane separation skid-mounted inlet separator, a separated liquid phase is merged into a liquid phase pipeline of the decarbonized oil-water separator, the separated gas phase is conveyed to a filter to be filtered and separated, the filtered liquid phase is merged into a liquid phase pipeline of the decarbonized oil-water separator, the filtered gas phase is used as a cold medium of the first heat exchanger, the cold medium is subjected to heat exchange and then passes through a heater, the temperature of the inlet membrane temperature is far away from a dew point and then is conveyed into the membrane separator, heated mixed gas is subjected to selective separation, permeation residual gas enters a low-carbon hydrocarbon recovery device, the permeation gas enters a residual gas compression system, and qualified permeation gas is obtained after compression and pressure is sent to a purified gas pipe network.
9. The method for extracting hydrogen by membrane separation at a low carbon hydrocarbon inlet section according to claim 8, wherein the heater adopts 0.6MPa steam for heating, and the gas phase is heated to 60-70 ℃ and then enters the membrane separator.
10. The method for extracting hydrogen through membrane separation at a low-carbon hydrocarbon inlet section according to claim 8, wherein the temperature of the permeation gas is reduced to 40 ℃ through a permeation gas cooler, the permeation gas is conveyed to a permeation gas compressor, the pressure of the permeation gas is increased to 3.4Mpa, and the permeation gas is conveyed to a purification gas pipe network, or the pressurized permeation gas is conveyed to a raw gas pipeline of a PSA hydrogen recovery device through a reflux cooler.
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