CN114854448B - Recovery device for liquefied gas in hydrogen production by reforming - Google Patents
Recovery device for liquefied gas in hydrogen production by reforming Download PDFInfo
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- CN114854448B CN114854448B CN202110147400.5A CN202110147400A CN114854448B CN 114854448 B CN114854448 B CN 114854448B CN 202110147400 A CN202110147400 A CN 202110147400A CN 114854448 B CN114854448 B CN 114854448B
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- 239000007789 gas Substances 0.000 title claims abstract description 151
- 239000001257 hydrogen Substances 0.000 title claims abstract description 147
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 147
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 238000002407 reforming Methods 0.000 title claims abstract description 36
- 238000011084 recovery Methods 0.000 title claims abstract description 30
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 29
- 238000010521 absorption reaction Methods 0.000 claims abstract description 83
- 238000000926 separation method Methods 0.000 claims abstract description 61
- 239000007791 liquid phase Substances 0.000 claims abstract description 15
- 239000000463 material Substances 0.000 claims abstract description 3
- 239000007788 liquid Substances 0.000 claims description 140
- 238000001816 cooling Methods 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 239000006096 absorbing agent Substances 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 239000000284 extract Substances 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 48
- 239000000047 product Substances 0.000 description 43
- 150000002431 hydrogen Chemical class 0.000 description 18
- 238000007906 compression Methods 0.000 description 15
- 230000006835 compression Effects 0.000 description 13
- 238000000034 method Methods 0.000 description 12
- 230000000694 effects Effects 0.000 description 8
- 238000005057 refrigeration Methods 0.000 description 5
- 238000001833 catalytic reforming Methods 0.000 description 4
- 239000002994 raw material Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000003209 petroleum derivative Substances 0.000 description 2
- 238000010926 purge Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G35/00—Reforming naphtha
- C10G35/24—Controlling or regulating of reforming operations
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/043—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by fractional condensation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
- C10G70/06—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes by gas-liquid contact
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The application discloses a recovery unit of liquefied gas in reforming hydrogen production belongs to the oil processing field. The device extracts reformate carried in reformate hydrogen for n times through n pressurizing liquid-separating devices connected in series to obtain extracted reformate hydrogen and n groups of mixed liquid phases; carrying out material separation on the n groups of mixed liquid phases through a product separation device to obtain separated liquefied gas and separated reformed generated oil; reversely contacting the extracted reformed hydrogen with the separated reformed oil through an absorption device to obtain contacted reformed oil; recovering the liquefied gas absorbed in the separated liquefied gas and the reformed oil after contact, wherein n is a positive integer. The device can simplify the flow of recovering the liquefied gas from the reformed hydrogen production, and improve the recovery efficiency of the liquefied gas.
Description
Technical Field
The application relates to the field of petroleum processing, in particular to a recovery device for liquefied gas in reforming hydrogen production.
Background
Catalytic reforming is a petroleum processing technology, which takes naphtha as raw material to carry out catalytic reforming and refine reforming generated oil, and simultaneously produces hydrogen as byproduct, namely reforming generated hydrogen.
The reformed hydrogen contains petroleum gas, and the liquefied gas can be recovered from the reformed hydrogen by a compression and cooling method in industry. The reformed hydrogen after the primary pressurization is cooled by an air cooler and then mixed with the reformed oil generated at the bottom of the No. 2 re-contact tank, the mixed reformed product (comprising the reformed oil and the reformed hydrogen) is further cooled and then enters the No. 1 re-contact tank, the gas-liquid balance is carried out in the No. 1 re-contact tank, the reformed oil which absorbs the liquefied gas is output at the bottom of the No. 1 re-contact tank, the reformed hydrogen generated at the top of the No. 1 re-contact tank is subjected to secondary compression according to the requirement of the sending pressure, the reformed oil generated at the bottom of the reformed product separation tank after the secondary compression is mixed again, the mixed reformed product enters the No. 2 re-contact tank for gas-liquid balance after being cooled by the cooler, the reformed oil generated at the bottom of the No. 2 re-contact tank is output, and the reformed oil is sent to the No. 1 re-contact tank.
In the recycling process of liquefied gas in hydrogen production by reforming, the liquefied gas needs to be mixed and contacted with the reformed oil for many times so as to contact and absorb the liquefied gas in hydrogen production by reforming, and the whole process is complex, high in energy consumption and poor in absorption effect.
Disclosure of Invention
The embodiment of the application provides a recovery device for liquefied gas in hydrogen production by reforming, which can simplify the flow of recovering liquefied gas from hydrogen production by reforming and improve the recovery efficiency of liquefied gas. The technical scheme is as follows:
according to one aspect of the present application, there is provided a recovery apparatus for liquefied gas in reformate hydrogen, the apparatus comprising an absorption apparatus, a product separation apparatus and n pressurized liquid separation apparatuses;
an i-level gas inlet for reforming hydrogen production is arranged on an i-th pressurizing liquid separating device in the n pressurizing liquid separating devices; the i-stage gas outlet of the i-th pressurized liquid separating device is connected with the i+1-stage gas inlet of the i+1-th pressurized liquid separating device; an n-level gas outlet of an n-th pressurized liquid separating device in the n pressurized liquid separating devices is connected with a gas inlet of an absorption device; the absorption device is provided with a purified gas outlet for reforming hydrogen production;
the liquid outlet of each of the n pressurized liquid separation devices is connected with the liquid inlet of the product separation device or with the liquid inlets of other downstream devices; the reformed product oil outlet of the product separation device is connected with the absorption liquid inlet of the absorption device; the absorption device is provided with an absorption liquid outlet for recycling the reformed oil; wherein i is a positive integer, n is a positive integer greater than 1, and i+1 is less than or equal to n.
According to another aspect of the present application, there is provided a recovery unit for liquefied gas in reformate hydrogen, the unit comprising 1 absorption unit, 1 product separation unit, 1 pressurized liquid separation unit and 1 intercooler;
the pressurizing liquid separating device comprises a first-stage supercharger, a first-stage air cooler, a first-stage water cooler and a first-stage liquid separating tank; the absorption device comprises a secondary booster, a tower top heat exchanger, a tower bottom heat exchanger and an absorption tower;
the primary booster is provided with a primary gas inlet for reforming hydrogen production, a booster outlet of the primary booster is connected with an air cooling inlet of a primary air cooler, an air cooling outlet of the primary air cooler is connected with a water cooling inlet of a primary water cooler, a water cooling outlet of the primary water cooler is connected with a liquid separating inlet of a primary liquid separating tank, a primary gas outlet arranged on the tank top of the primary liquid separating tank is connected with a secondary gas inlet on the secondary booster, and a liquid outlet arranged on the tank bottom of the primary liquid separating tank is connected with a liquid inlet of a product separating device or connected with liquid inlets of other downstream devices;
the second-stage booster is characterized in that a booster outlet of the second-stage booster is connected with a first heat exchange inlet of a tower bottom heat exchanger, a first heat exchange outlet of the tower bottom heat exchanger is connected with a first heat exchange inlet of a tower top heat exchanger, a first heat exchange outlet of the tower top heat exchanger is connected with a gas inlet arranged at the lower part of a tower body of the absorption tower, a reformed oil outlet in the product separation device is connected with an absorption liquid inlet arranged at the upper part of the tower body of the absorption tower through an intercooler, a tower bottom liquid outlet of the absorption tower is connected with a second heat exchange inlet of the tower bottom heat exchanger, and a tower top gas outlet of the absorption tower is connected with a second heat exchange inlet of the tower top heat exchanger;
the tower bottom heat exchanger is provided with an absorption liquid outlet for reforming generated oil, and the tower top heat exchanger is provided with a purified gas outlet for reforming generated hydrogen.
The beneficial effects that technical scheme that this application embodiment provided include at least:
the recovery device of liquefied gas in the reformed hydrogen production is used for compressing the reformed hydrogen production in the forward direction through the pressurizing liquid separating device, liquefying a mixed liquid phase from the reformed hydrogen production, separating the liquefied gas and the reformed generated oil from the mixed liquid phase through the product separating device, and rapidly separating the liquefied gas from the reformed hydrogen production; and then, reversely contacting the reformed hydrogen separated by the pressurizing liquid separation device with the reformed product oil separated by the product separation device, and re-absorbing the liquefied gas from the separated reformed hydrogen, namely, secondarily separating the liquefied gas in the reformed hydrogen, wherein the liquefied gas can be rapidly recovered by combining a gas compression mode with an absorption mode of the reformed product oil, the liquefied gas in the reformed hydrogen is not required to be absorbed by the reformed product oil for multiple times, the flow of recovering the liquefied gas from the reformed hydrogen is simplified, the recovery efficiency of the liquefied gas is improved, and the yields of the liquefied gas and the reformed product oil and the purification effect of the reformed hydrogen are also improved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the description of the embodiments will be briefly introduced below, and it is obvious that the drawings in the following description are only some embodiments of the present application, and that other drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
Fig. 1 is a schematic structural view showing a liquefied gas recovery apparatus in reforming hydrogen according to an exemplary embodiment of the present application;
fig. 2 is a schematic structural view showing a liquefied gas recovery apparatus in reforming hydrogen according to another exemplary embodiment of the present application;
fig. 3 is a schematic view showing the construction of a conventional liquefied gas recovery apparatus for reforming hydrogen according to an exemplary embodiment of the present application.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present application more apparent, the embodiments of the present application will be described in further detail below with reference to the accompanying drawings.
First, several terms referred to in this application are described:
catalytic reforming is an important oil refining process for producing high-octane gasoline and light aromatic hydrocarbon (benzene, toluene and xylene) by using naphtha as a raw material and simultaneously producing hydrogen as a byproduct; the oil refined by catalytic reforming is the reformed oil, and the byproduct hydrogen is the reformed hydrogen.
Naphtha refers to light oil which is produced by processing crude oil or other raw materials and is used for chemical raw materials.
Liquefied petroleum gas, also called as liquefied gas, is a colorless volatile liquid product obtained by pressurizing, cooling and liquefying gas (such as petroleum gas) generated and recovered in the refining process of oil refining. The main components are propane, butane, propylene and butylene.
FIG. 1 shows a schematic diagram of a device for recovering liquefied gas from reformed hydrogen according to an exemplary embodiment of the present application, which includes an absorption device 120, a product separation device 140, and n pressurized liquid separation devices 160;
an i-stage gas inlet for reforming hydrogen production is arranged on the i-th pressurizing liquid separating device 160 in the n pressurizing liquid separating devices 160; the i-stage gas outlet of the i-th pressurized liquid separation device 160 is connected with the i+1-stage gas inlet of the i+1-th pressurized liquid separation device 160; the n-stage gas outlet of the nth pressurized liquid separator 160 of the n pressurized liquid separators 160 is connected with the gas inlet of the absorbing device 120; the absorption device 120 is provided with a purified gas outlet for reforming hydrogen production;
the liquid outlet of each of the n pressurized liquid separation devices 160 is connected to the liquid inlet of the product separation device 140 or to the liquid inlets of other downstream devices; the reformate outlet of the product separation apparatus 140 is connected to the absorption liquid inlet of the absorption apparatus 120; the absorption device 120 is provided with an absorption liquid outlet for recovering the reformed oil; wherein i is a positive integer, n is a positive integer greater than 1, and i+1 is less than or equal to n.
In some embodiments, the ith pressurized liquid separator 160 includes an i-stage booster 162, an i-stage cooler 164, and an i-stage liquid separator tank 166;
the i-stage gas inlet of the i-th pressurized liquid separator 160 of the n pressurized liquid separators 160 is arranged on the i-stage booster 162, the booster outlet of the i-stage booster 162 is connected with the cooling inlet of the i-stage cooler 164, the cooling outlet of the i-stage cooler 164 is connected with the liquid separating inlet of the i-stage liquid separator 166, and the i-stage gas outlet arranged on the tank top of the i-stage liquid separator 166 is connected with the i+1-stage gas inlet; the liquid outlet provided on the bottom of the i-stage liquid tank 166 is connected to the liquid inlet of the product separation device 140 or to the liquid inlet of other downstream devices. The liquid outlet provided at the bottom of the i-stage liquid tank 166 is the liquid outlet of the pressurized liquid separator 160.
In some embodiments, the i-stage cooler 164 comprises at least one of an air cooler, a water cooler, and a heat exchanger.
In some embodiments, absorption unit 120 includes an n+1 stage booster 122, a bottom heat exchanger 124, an overhead heat exchanger 126, and an absorption column 128;
the gas inlet of the absorber 120 is disposed on the n+1 stage booster 122, the booster outlet of the n+1 stage booster 122 is connected with the first heat exchange inlet of the bottom heat exchanger 124, the first heat exchange outlet of the bottom heat exchanger 124 is connected with the first heat exchange inlet of the top heat exchanger 126, the first heat exchange outlet of the top heat exchanger 126 is connected with the gas inlet disposed at the lower part of the body of the absorber 128, the reformed oil outlet is connected with the absorption liquid inlet disposed at the upper part of the body of the absorber 128, the bottom liquid outlet of the absorber 128 is connected with the second heat exchange inlet of the bottom heat exchanger 124, the top gas outlet of the absorber 128 is connected with the second heat exchange inlet of the top heat exchanger 126, the bottom heat exchanger 124 is provided with the absorption liquid outlet, and the top heat exchanger 126 is provided with the purified gas outlet.
In some embodiments, the reformate outlet and the absorption liquid inlet are connected by an intercooler 180; the intercooler 180 is used to cool the temperature of the reformate output from the reformate outlet to a temperature interval of 0 to 40 degrees celsius, the temperature interval including 0 degrees celsius and 40 degrees celsius.
In some embodiments, absorber 128 is a tray column or a packed column.
In some embodiments, the gas pressure value of the purge gas outlet falls within a range of gas pressure values for the hydrogen network.
Describing the process of recovering liquefied gas in the reformed hydrogen by using the recovery device, firstly, the reformed hydrogen enters the recovery device from a first-stage gas inlet of a first-stage pressurizing and liquid-separating device 160, and the reformed hydrogen passes through a first-stage supercharger 162 to obtain the pressurized reformed hydrogen; the pressurized reformed hydrogen enters a primary cooler 164 for cooling to obtain cooled reformed hydrogen; the cooled reformed hydrogen enters a first-stage liquid separating tank 166 for liquid separation treatment, the 1 st group of mixed liquid phase flows out from the tank bottom of the first-stage liquid separating tank 166, and the first-stage reformed hydrogen flows out from the tank top of the first-stage liquid separating tank 166; the 1 st mixed liquid phase flows into the product separation device 140 for substance separation, the first-stage reformed hydrogen enters the second-stage booster 162, the compression, cooling and liquid separation processes of the reformed hydrogen in the first-stage pressurizing and liquid separation device 160 are repeated in the remaining n-1 pressurizing and liquid separation devices 160, 1 st mixed liquid phase flows out of each pressurizing and liquid separation device 160 into the product separation device 140, the i-stage reformed hydrogen flowing out of the i-stage pressurizing and liquid separation device 160 enters the i+1-stage booster 162 of the i-stage pressurizing and liquid separation device 160, and the n-stage reformed hydrogen flowing out of the n-stage pressurizing and liquid separation device 166 of the n-stage pressurizing and liquid separation device 160 (namely, the reformed hydrogen after extraction) flows into the absorption device 120.
The n groups of mixed liquid phases contain reforming generated oil and liquefied gas; the n groups of mixed liquid phases sequentially enter the product separation device 140 to perform material separation, liquefied gas and reformed product oil are separated from the mixed liquid phases, and the separated liquefied gas and the separated reformed product oil flow out of the product separation device 140. The separated reformate flowing out of the product separator 140 is cooled by the intercooler 180 and then enters the absorber 120, and the separated reformate is used as an absorption liquid for liquefied gas in the extracted reformate hydrogen.
The extracted reformed hydrogen enters the absorption device 120 from a gas inlet on the n+1-stage booster 122, pressurized reformed hydrogen is obtained after compression treatment of the n+1-stage booster 122, the pressurized reformed hydrogen enters a tower bottom heat exchanger 124 at the bottom of the absorption tower, then enters a tower top heat exchanger 126 at the top of the absorption tower after passing through the tower bottom heat exchanger 124, the pressurized reformed hydrogen is cooled through twice heat exchange, then the cooled reformed hydrogen enters the absorption tower from a gas inlet arranged at the lower part of the tower body of the absorption tower 128, the separated reformed hydrogen enters the absorption tower 128 from an absorption liquid inlet arranged at the upper part of the tower body of the absorption tower 128, the cooled reformed hydrogen flows upwards from the lower part of the absorption tower 128, the separated reformed hydrogen flows downwards from the upper part of the absorption tower 128, and the extracted reformed hydrogen and the separated reformed hydrogen are in reverse contact, so that the separated reformed hydrogen fully absorbs liquefied gas from the extracted reformed hydrogen.
Separately recovering the liquefied gas and the reformed oil, and separating the separated reformed oil to obtain the liquefied gas and the reformed oil, storing the liquefied gas in a liquefied gas storage device, and storing the reformed oil in a reformed oil storage device; alternatively, the separated reformate is directly recovered.
The hydrogen pipe network is a transmission network of hydrogen, the absorption device absorbs liquefied gas in the extracted reformed hydrogen to obtain purified reformed hydrogen, and the purified reformed hydrogen is input into the hydrogen pipe network according to a specified gas pressure value range.
Illustratively, the series of levels of the above-described levels, i, … …, n, represent gas pressure levels, wherein the levels exhibit a positive correlation with gas pressure, e.g., the gas pressure of the i+1 level is greater than the gas pressure of the i level.
For example, the cooler 164 may be a combination of coolers, for example, the cooler 164 is formed by combining an air cooler and a water cooler in series, when cooling the pressurized reformed hydrogen, the air cooler first cools the pressurized reformed hydrogen, then the cooled reformed hydrogen enters the water cooler, the water cooler secondarily cools the cooled reformed hydrogen, and finally the secondarily cooled reformed hydrogen enters the liquid separation tank.
Illustratively, the intercooler 180 may be a refrigeration system. When the pressure of the absorption tower is constant, the lower the temperature of the reformed oil entering the absorption tower 128, the better the absorption effect of the liquefied gas in the reformed hydrogen, the higher the purification degree of the reformed hydrogen, and the temperature of the refrigeration system may be set according to the negative correlation between the purification degree of the reformed hydrogen and the temperature of the reformed oil, for example, the lower the temperature of the refrigeration system is set when the purification degree of the reformed hydrogen is required to be higher. Illustratively, the refrigeration system is set in a temperature range of 0 to 40 degrees celsius.
Illustratively, the gas inlet of the absorber 128 is disposed at a position of the tower body near the bottom of the tower, and the absorption liquid inlet of the absorber 128 is disposed at a position of the tower body near the top of the tower.
The specified pressure value range refers to the gas pressure value range of the hydrogen pipe network, that is, the gas pressure value of the purified gas outlet belongs to the gas pressure value range of the hydrogen pipe network. The adjustment of the gas pressure may be, for example, by way of compression adjustment. Optionally, the gas pressure of the hydrogen pipe network is in a range of 1Mpa to 4Mpa, wherein Mpa is the unit megapascal pressure, and g is the pressure indicated by the pressure gauge, namely gauge pressure. For example, the compression level j+1 of the reformed hydrogen may be set according to the pressure of the hydrogen pipe network, where the compression level of the reformed hydrogen is in positive correlation with the purity, that is, the higher the compression level of the reformed hydrogen is, the higher the pressure at the time of outputting the reformed hydrogen is, the higher the purity of the reformed hydrogen is, and the higher the energy consumption is.
By way of example, other downstream devices refer to other equipment for the treatment of reformate, such as an olefin extraction device for reformate.
In summary, the recovery device for liquefied gas in reformed hydrogen provided in this embodiment compresses the reformed hydrogen in the forward direction by the pressurizing liquid-separating device, and liquefies the mixed liquid phase from the reformed hydrogen; and then, reversely contacting the reformed hydrogen produced by the pressure liquid separation device with the reformed product oil separated by the product separation device, and re-absorbing the liquefied gas from the separated reformed hydrogen produced by the reforming product oil, namely, secondarily separating the liquefied gas in the reformed hydrogen produced by the secondary separation. The device can rapidly recycle the liquefied gas by combining a gas compression mode and an absorption mode of the reformed product oil, does not need to absorb the liquefied gas in the reformed hydrogen through the reformed product oil for multiple times, simplifies the flow of recycling the liquefied gas from the reformed hydrogen, improves the recycling efficiency of the liquefied gas, and also improves the yield of the liquefied gas and the reformed product oil and the purification effect of the reformed hydrogen. In addition, because the reformed hydrogen is not mixed with the reformed oil in the compression process, the risk of coking of the cylinder of the reformed hydrogen compressor is reduced.
FIG. 2 shows a schematic structural diagram of a liquefied gas recovery unit for reforming hydrogen according to another exemplary embodiment of the present application, which includes 1 absorption unit 320, 1 product separation unit 340, 1 pressurized liquid separation unit 360, and 1 intercooler 380;
the pressurized liquid separation device 360 comprises a primary booster 362, a primary air cooler 364, a primary water cooler 366 and a primary liquid separation tank 368; the absorber 320 comprises a secondary booster 322, a bottom heat exchanger 324, a top heat exchanger 326 and an absorber 328;
the primary booster 362 is provided with a primary gas inlet for reforming hydrogen production, a booster outlet of the primary booster 362 is connected with an air cooling inlet of the primary air cooler 364, an air cooling outlet of the primary air cooler 364 is connected with a water cooling inlet of the primary water cooler 366, a water cooling outlet of the primary water cooler 366 is connected with a liquid separating inlet of the primary liquid separating tank 368, a primary gas outlet arranged on the tank top of the primary liquid separating tank 368 is connected with a secondary gas inlet on the secondary booster 322, and a liquid outlet arranged on the tank bottom of the primary liquid separating tank 368 is connected with a liquid inlet of the product separating device 340 or connected with liquid inlets of other downstream devices;
the pressurizing outlet of the secondary pressurizing machine 322 is connected with a first heat exchange inlet of a tower bottom heat exchanger 324, a first heat exchange outlet of the tower bottom heat exchanger 324 is connected with a first heat exchange inlet of a tower top heat exchanger 326, a first heat exchange outlet of the tower top heat exchanger 326 is connected with a gas inlet arranged at the lower part of a tower body of the absorption tower 328, a reformed oil outlet in the product separating device 340 is connected with an absorption liquid inlet arranged at the upper part of the tower body of the absorption tower 328 through an intercooler 380, a tower bottom liquid outlet of the absorption tower 328 is connected with a second heat exchange inlet of the tower bottom heat exchanger 324, and a tower top gas outlet of the absorption tower 328 is connected with the second heat exchange inlet of the tower top heat exchanger 326;
the bottom heat exchanger 324 is provided with an absorption liquid outlet for the reformate, and the top heat exchanger 326 is provided with a purified gas outlet for the reformate.
In some embodiments, the intercooler 380 is configured to cool the reformate output from the reformate outlet to a temperature in the range of 0 to 40 degrees celsius, where the temperature range includes 0 degrees celsius and 40 degrees celsius.
In some embodiments, absorber 328 is a tray column or a packed column.
In some embodiments, the gas pressure value of the purge gas outlet falls within a range of gas pressure values for the hydrogen network.
In summary, the recovery device for liquefied gas in reformed hydrogen provided in this embodiment compresses the reformed hydrogen in the forward direction by the pressurizing liquid-separating device, and liquefies the mixed liquid phase from the reformed hydrogen; and then, reversely contacting the reformed hydrogen produced by the pressure liquid separation device with the reformed product oil separated by the product separation device, and re-absorbing the liquefied gas from the separated reformed hydrogen produced by the reforming product oil, namely, secondarily separating the liquefied gas in the reformed hydrogen produced by the secondary separation. The device can rapidly recycle the liquefied gas by combining a gas compression mode and an absorption mode of the reformed product oil, does not need to absorb the liquefied gas in the reformed hydrogen through the reformed product oil for multiple times, simplifies the flow of recycling the liquefied gas from the reformed hydrogen, improves the recycling efficiency of the liquefied gas, and also improves the yield of the liquefied gas and the reformed product oil and the purification effect of the reformed hydrogen. In addition, because the reformed hydrogen is not mixed with the reformed oil in the compression process, the risk of coking of the cylinder of the reformed hydrogen compressor is reduced.
Illustratively, on a continuous reforming scale of 100 ten thousand tons/year, the pressure of the outgoing hydrogen (i.e., the pressure of the reformed hydrogen supplied to the hydrogen pipe network) was 2.7mpa, and two-stage compression was required for the reformed hydrogen, the recovery effect of the liquefied gas in the reformed hydrogen was verified, i.e., the effect was verified based on the apparatus shown in fig. 2, and experimental data shown in tables 1 and 2 were obtained. Compared with the traditional recovery method of liquefied gas in hydrogen production by reforming, the recovery method of liquefied gas in hydrogen production provided by the application can obviously obtain that more liquefied gas can be recovered, and compared with the traditional recovery method (the device adopted by the traditional recovery method is shown in the figure 3), the liquefied gas in the reformed product oil recovered by the recovery method of the application is increased by 56%, and the purity of hydrogen is also purified to 95.6%. Wherein C5+ refers to hydrocarbons having a carbon number of greater than or equal to 5.
TABLE 1
| Hydrogen production, kg/hr (kg/h) | Purity of hydrogen, mole (mol) | |
| Traditional recovery method | 10022 | 94.7％ |
| Recovery method of the present application | 8779 | 95.6％ |
TABLE 2
By way of example, the icon in fig. 3 is illustrated as follows: 501, a first stage compressor; 502, an air cooler; 503, a water cooler; 504,1 re-contact tank; 505, a secondary compressor; 506, an air cooler; 507, a water cooler; 508, a refrigeration system; 509,2 the tank is contacted again.
In summary, the recovery device for liquefied gas in hydrogen production by reforming provided by the application has better effect of recovering liquefied gas and reformate from hydrogen production by reforming, and can also improve the purity of hydrogen production by reforming.
It should be understood that references herein to "a plurality" are to two or more. "and/or", describes an association relationship of an association object, and indicates that there may be three relationships, for example, a and/or B, and may indicate: a exists alone, A and B exist together, and B exists alone. The character "/" generally indicates that the context-dependent object is an "or" relationship.
The foregoing description of the preferred embodiments is merely exemplary in nature and is in no way intended to limit the invention, since it is intended that all modifications, equivalents, improvements, etc. that fall within the spirit and scope of the invention.
Claims (8)
1. The device is characterized by comprising an absorption device, a product separation device and n pressurizing liquid separation devices;
an i-level gas inlet for reforming hydrogen production is arranged on an i-th pressurizing liquid separating device in the n pressurizing liquid separating devices; the i-stage gas outlet of the i-th pressurized liquid separating device is connected with the i+1-stage gas inlet of the i+1-th pressurized liquid separating device; an n-level gas outlet of an n-th pressurized liquid separating device in the n pressurized liquid separating devices is connected with a gas inlet of the absorption device; the absorption device is provided with a purified gas outlet for reforming hydrogen production;
the liquid outlet of each of the n pressurized liquid separation devices is connected with the liquid inlet of the product separation device or with the liquid inlets of other downstream devices; the reformed product oil outlet of the product separation device is connected with the absorption liquid inlet of the absorption device; an absorption liquid outlet for recycling the reformed oil is arranged on the absorption device; wherein i is a positive integer, n is a positive integer greater than 1, and i+1 is less than or equal to n;
the ith pressurizing liquid separating device comprises an i-stage supercharger, an i-stage cooler and an i-stage liquid separating tank;
an i-stage gas inlet of an i-th pressurizing and separating device in the n pressurizing and separating devices is arranged on the i-stage supercharger, a supercharging outlet of the i-stage supercharger is connected with a cooling inlet of the i-stage cooler, a cooling outlet of the i-stage cooler is connected with a separating inlet of the i-stage liquid tank, and an i-stage gas outlet arranged on the top of the i-stage liquid tank is connected with the i+1-stage gas inlet; a liquid outlet arranged on the tank bottom of the i-stage liquid tank is connected with a liquid inlet of the product separation device or connected with a liquid inlet of the other downstream devices;
the reformed hydrogen enters the recovery device from the i-stage gas inlet of the pressurizing liquid separating device, and the reformed hydrogen passes through the i-stage supercharger to obtain the pressurized reformed hydrogen; the pressurized reformed hydrogen enters the i-stage cooler to be cooled, so that cooled reformed hydrogen is obtained; the cooled reformed hydrogen enters the i-stage liquid tank for liquid separation treatment, a group of mixed liquid phases flow out from the tank bottom of the i-stage liquid tank, a group of reformed hydrogen flows out from the tank top of the i-stage liquid tank, and the i-stage reformed hydrogen flowing out from the i-stage liquid tank of the i-stage pressurizing and liquid separating device enters an i+1-stage supercharger of the i+1-stage pressurizing and liquid separating device;
the group of mixed liquid phases flowing out of each pressurizing liquid separation device enter the product separation device to carry out material separation, liquefied gas and reformed product oil are separated from the mixed liquid phases, and the separated reformed product oil flowing out of the product separation device enters the absorption device;
the absorption device comprises an n+1-level booster, a tower top heat exchanger, a tower bottom heat exchanger and an absorption tower;
the gas inlet of the absorption device is arranged on the n+1-stage supercharger, the supercharging outlet of the n+1-stage supercharger is connected with the first heat exchange inlet of the tower bottom heat exchanger, the first heat exchange outlet of the tower bottom heat exchanger is connected with the first heat exchange inlet of the tower top heat exchanger, the first heat exchange outlet of the tower top heat exchanger is connected with the gas inlet arranged at the lower part of the tower body of the absorption tower, the reformed oil outlet is connected with the absorption liquid inlet arranged at the upper part of the tower body of the absorption tower, the tower bottom liquid outlet of the absorption tower is connected with the second heat exchange inlet of the tower bottom heat exchanger, the tower top gas outlet of the absorption tower is connected with the second heat exchange inlet of the tower top heat exchanger, the absorption liquid outlet is arranged on the tower bottom heat exchanger, and the purification gas outlet is arranged on the tower top heat exchanger.
2. The apparatus of claim 1, wherein the i-stage cooler comprises at least one of an air cooler, a water cooler, and a heat exchanger.
3. The apparatus of claim 1, wherein the reformate outlet is connected to the absorption liquid inlet by an intercooler; the intercooler is used for cooling the temperature of the reformed oil output by the reformed oil outlet to a temperature interval of 0-40 ℃, wherein the temperature interval comprises 0-40 ℃.
4. The apparatus of claim 1, wherein the absorber column is a tray column or a packed column.
5. The apparatus of claim 1, wherein the purified gas outlet has a gas pressure rating that falls within a gas pressure rating range of a hydrogen pipe network.
6. A recovery device of liquefied gas in reforming hydrogen production, which is characterized by comprising 1 absorption device, 1 product separation device, 1 pressurizing liquid separation device and 1 intercooler;
the pressurizing liquid separating device comprises a first-stage supercharger, a first-stage air cooler, a first-stage water cooler and a first-stage liquid separating tank; the absorption device comprises a secondary booster, a tower top heat exchanger, a tower bottom heat exchanger and an absorption tower;
the primary booster is provided with a primary gas inlet for reforming hydrogen production, a booster outlet of the primary booster is connected with an air cooling inlet of the primary air cooler, an air cooling outlet of the primary air cooler is connected with a water cooling inlet of the primary water cooler, a water cooling outlet of the primary water cooler is connected with a liquid separating inlet of the primary liquid separating tank, a primary gas outlet arranged on the tank top of the primary liquid separating tank is connected with a secondary gas inlet on the secondary booster, and a liquid outlet arranged on the tank bottom of the primary liquid separating tank is connected with a liquid inlet of the product separating device or connected with liquid inlets of other downstream devices;
the second-stage booster is characterized in that a booster outlet of the second-stage booster is connected with a first heat exchange inlet of the tower bottom heat exchanger, a first heat exchange outlet of the tower bottom heat exchanger is connected with a first heat exchange inlet of the tower top heat exchanger, a first heat exchange outlet of the tower top heat exchanger is connected with a gas inlet arranged at the lower part of a tower body of the absorption tower, a reformed oil outlet in the product separation device is connected with an absorption liquid inlet arranged at the upper part of the tower body of the absorption tower through the intercooler, a tower bottom liquid outlet of the absorption tower is connected with a second heat exchange inlet of the tower bottom heat exchanger, and a tower top gas outlet of the absorption tower is connected with a second heat exchange inlet of the tower top heat exchanger;
the tower bottom heat exchanger is provided with an absorption liquid outlet for reforming generated oil, and the tower top heat exchanger is provided with a purified gas outlet for reforming generated hydrogen.
7. The apparatus of claim 6, wherein the intercooler is configured to cool the reformate output from the reformate outlet to a temperature range of 0 to 40 degrees celsius, the temperature range including 0 degrees celsius and 40 degrees celsius.
8. The apparatus of claim 6, wherein the absorber column is a tray column or a packed column.
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