CN108795491B - Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower - Google Patents
Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower Download PDFInfo
- Publication number
- CN108795491B CN108795491B CN201710306524.7A CN201710306524A CN108795491B CN 108795491 B CN108795491 B CN 108795491B CN 201710306524 A CN201710306524 A CN 201710306524A CN 108795491 B CN108795491 B CN 108795491B
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- pipeline
- light component
- hydrogen
- heat exchanger
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
-
- 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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a coupling system of a reforming full-distillate liquid-phase product hydrogenation device and a light component removal tower, which comprises the following components: a hydrogenation device and a light component removing tower; the hydrogenation device is in coupling relation with the light component removal tower and comprises a heat exchanger A arranged on a hydrogenation product removal pipeline, a heat exchanger B arranged on a tower bottom heavy component removal pipeline, wherein the hydrogenation product removal pipeline is communicated with the heat exchanger A and then is communicated with the heat exchanger B through a pipeline, and finally, the hydrogenation product removal pipeline is communicated with the light component removal tower through a feeding pipeline of the light component removal tower. The invention solves the problem of influence of temperature rise of the hydrogenation device on the operation of the light component removal tower on the basis of the prior art, is beneficial to stable operation of the device and prolongs the operation period.
Description
Technical Field
The invention relates to a coupling system of a reforming full-fraction liquid-phase product hydrogenation device and a light component removal tower, in particular to a system for removing hydrocarbons containing carbon-carbon double bonds and/or carbon-carbon triple bonds by liquid-phase hydrogenation of a reforming reaction liquid-phase product.
Background
Catalytic reforming (Catalytic Reforming) is one of the main processes for petroleum refining. The method is a process for converting naphtha into reforming reaction liquid phase products rich in aromatic hydrocarbon and producing hydrogen as a byproduct under the conditions of certain temperature, pressure, hydrogen and the presence of a catalyst. The reforming reaction liquid phase product can be directly used as a blending component of the motor gasoline, and can also be used for preparing one of benzene, toluene and xylene through aromatic hydrocarbon extraction, and byproduct hydrogen is one of main sources of hydrogen for hydrogenation devices (such as hydrofining, hydrocracking and the like) of oil refineries.
Since 1940's first set of hydrogen-bearing reforming process units was put into production, catalytic reforming processes have been developed over nearly 60 years so far, and many countries have continuously developed and studied catalytic reforming processes as the market and human life demand for fuels and aromatics.
The development of the catalytic reforming process should include two parts: namely, the development of the catalytic reforming process and the development of the catalytic reforming catalyst complement each other, and the development of the catalytic reforming catalyst is indispensable. The catalytic reforming catalyst determines the speed and depth of the catalytic reforming reaction process, which is the most important factor in the catalytic reforming process, and the development of the catalytic reforming catalyst supports the development of the catalytic reforming process. In contrast, the development of the catalytic reforming process has also driven the further development and research of catalytic reforming catalysts.
In recent years, along with the development of reforming catalysts and catalytic reforming processes, the introduction of efficient equipment such as a countercurrent vertical heat exchanger, a multi-flow-path combined heating furnace and the like improves the process flow, reduces the pressure drop of a hydrogenation system, and greatly reduces the hydrogenation pressure of catalytic reforming; meanwhile, the energy consumption is reduced, and the product yield is improved. As the reaction pressure of the reforming device is further reduced, the reaction severity is further improved, so that the liquid phase product of the reforming reaction is rich in a large amount of unsaturated hydrocarbons, such as hydrocarbons containing carbon-carbon double bonds or carbon-carbon triple bonds, and the stable operation and the product quality of the subsequent aromatic extraction device are seriously affected. The reforming reaction liquid phase product therefore typically requires pretreatment prior to entering the aromatic hydrocarbon pump. At present, a large number of reforming devices in China still adopt a clay pretreatment process. The clay pretreatment process has the problems of poor refining depth, large heavy component yield, quick clay deactivation and the like, and particularly has serious environmental pollution risks in the treatment of deactivated waste clay, so that a refining enterprise faces huge environmental protection pressure.
In recent years, there have been reports about process technology for the selective hydrogenation removal of olefins from liquid phase products of reforming reactions (arowing process for IFP in france). Benzene fraction of reforming reaction liquid phase product is used as raw material, noble metal catalyst is used, and olefine in raw material is removed under the condition of moderate reaction. Industrial application of the liquid-phase product BTX fraction and full fraction selective hydrogenation olefin removal technology of catalytic reforming reaction has not been reported at home and abroad.
The chinese petrochemical company, inc. Strongpoint petrochemical institute developed a selective hydrodeolefination technology (FHDO) for catalytic reforming of liquid phase products using noble metal catalysts. The FHDO technology in 2003 is successfully applied to benzene fraction hydrodeolefine device of the name petrochemical company; the industrial application of the industrial device for selectively hydrodeolefine of the BTX fraction of the Yanshan and the BTX fraction of the Changling company is successfully realized in 2005; in 2009, the method can be applied to industrial equipment for the full-fraction selective hydrodeolefination of the liquid-phase product of the ballasted reforming reaction. The device for selectively hydrogenating and removing olefin from the reforming reaction liquid-phase product is provided with a raw material pump, a new hydrogen compressor, a circulating hydrogen compressor and other movable equipment, and hydrogen of the device is circularly operated. The circulation of hydrogen not only brings higher energy consumption of the device, but also forms temperature rise in the reactor, thereby causing partial saturation of aromatic hydrocarbon and affecting the economic benefit of enterprises.
CN103666544B discloses a method for hydrotreating a reformate, which comprises contacting the reformate with a catalyst having a catalytic hydrogenation effect in a hydrogenation reactor under liquid phase hydrotreating conditions, wherein hydrogen used in the hydrotreating is at least partially derived from dissolved hydrogen in the reformate, and the hydrogenation reaction product directly enters a light component removal column. According to this method, the reformate separated from the reformate separation tank is directly subjected to liquid phase hydrotreatment, and dissolved hydrogen in the reformate is fully utilized, so that the device configuration is simple. In practice, the following disadvantages exist: (1) In order to strengthen the liquid-phase hydrogenation reaction, the reformed product oil obtained by separating in a reformed product separating tank enters a hydrogenation reactor, and the person skilled in the art knows that the gas phase obtained by separating in the reformed product separating tank still contains more light hydrocarbon components, and other devices are needed to recycle the light hydrocarbon components, so that the reforming system device and the working condition are not fully utilized; (2) In order to meet the temperature requirement of the light component removal tower, the temperature of the hydrogenation reaction device can be adjusted only in a small range, and generally cannot meet the requirement of raising the temperature after the activity of the catalyst is reduced to reach the required reaction depth. CN203878113U discloses a reforming reaction liquid phase product hydrogenation system. The system comprises a hydrogenation reactor, wherein the hydrogenation reactor is arranged between a reforming re-contactor and a stabilizer, high-purity hydrogen obtained by utilizing the re-contactor is mixed with bottom oil of the re-contactor, and then an online liquid-phase hydrogenation reaction is carried out in the hydrogenation reactor, and a reaction product enters the stabilizer again. The system can carry out deep selective hydrogenation reaction on the reforming reaction liquid phase product under milder process conditions; because the hydrogenation reactor is arranged between the re-contactor and the stabilizer, the hydrogen obtained by the re-contactor can be directly used as a hydrogen source, and the reaction of removing carbon-carbon double bonds or carbon-carbon triple bonds hydrocarbon by hydrogenation is carried out under the condition of liquid phase hydrogenation, thereby omitting a circulating hydrogen compressor in the existing hydrogenation system and greatly reducing investment cost and operation cost. The system has the following defects: the hydrogenation reaction product directly enters the light component removing tower, so that the hydrogenation reaction temperature is limited by the feeding temperature of the light component removing tower and cannot be adjusted in a large range to adapt to the required reaction temperature adjustment of the activity change of the catalyst.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a coupling system of a reforming full-fraction liquid-phase product hydrogenation device and a light component removal tower, which is used for hydrogenating a catalytic reforming reaction liquid-phase product to remove carbon-carbon double bonds and/or carbon-carbon triple bond hydrocarbon impurities so as to meet the limitation of an aromatic hydrocarbon extraction device on the content of carbon-carbon double bonds or carbon-carbon triple bond hydrocarbon in the catalytic reforming reaction liquid-phase product, and meanwhile, the reaction temperature of the hydrogenation reaction device can be adjusted in a larger range according to the reaction requirement, and the normal operation of the light component removal tower coupled with the hydrogenation device is not influenced.
The technical scheme provided by the invention is as follows:
a reformate full distillate liquid phase product hydrogenation unit and light ends removal column coupling system comprising:
a hydrogenation unit comprising a feed line for introducing a hydrogenation unit feed to the hydrogenation reaction unit and a hydrogenation product removal line for removing hydrogenation products;
a light ends column comprising a feed line for introducing a light ends column feed to the light ends column, and a removal line for removing overhead light ends obtained after fractionation, and a removal line for removing bottom heavy ends obtained after fractionation;
the hydrogenation device is in coupling relation with the light component removing tower, and comprises a heat exchanger A (for reducing the temperature of a hydrogenation product) arranged on a hydrogenation product removing pipeline, a heat exchanger B (for increasing the temperature of the hydrogenation product) arranged on a tower bottom heavy component removing pipeline, wherein the hydrogenation product removing pipeline is communicated with the heat exchanger A and then is communicated with the heat exchanger B through a pipeline, and finally, the hydrogenation product removing pipeline is communicated with the light component removing tower through a feeding pipeline of the light component removing tower.
In the invention, the cold material of the heat exchanger A is fed by a hydrogenation device, and the hot material of the heat exchanger B is the heavy component at the bottom of the light component removing tower.
In the invention, a pre-hydrogenation device can be arranged in front of the hydrogenation device, the operation is carried out at a temperature lower than that of the hydrogenation device, an outlet pipeline of the pre-hydrogenation device is communicated with the heat exchanger A, and the reformed full-fraction liquid phase product firstly passes through the pre-hydrogenation device to be pre-hydrogenated, and then is hydrogenated in the hydrogenation device.
In the invention, the hydrogenation device and/or the pre-hydrogenation device are/is provided with a hydrogen supplementing pipeline and a hydrogen quantity control device, and the supplementing hydrogen quantity is determined according to the reaction requirement, but the premise is that the operation of the light component removing tower is not seriously influenced. The make-up hydrogen can be supplemented into the hydrogenation unit feed by a gas-liquid mixer, or can be mixed by a pipeline or assisted by other existing devices (such as a heat exchanger, etc.).
In the invention, a heating device and a temperature control device are arranged on a feeding pipe line of the hydrogenation device and are used for regulating and controlling the reaction temperature of the hydrogenation device, and the heating device and the temperature control device are generally arranged behind a heat exchanger A. The heating device can be a heating furnace, a steam heater, an electric heater, a heat conducting oil heater and the like.
In the present invention, the reforming whole fraction liquid phase product generally comprises a suitable raw material from which reformer light hydrocarbons (light hydrocarbons in reformed hydrogen, light hydrocarbons in the top gas of a light component removal column, etc.) are recovered, and other sources can be supplemented. The re-contactor (re-contacting the reformed oil with the reformed hydrogen to recover the light hydrocarbon therein), the impurity removal tank (such as a dechlorination tank), the liquefied gas recovery tank and the like may be provided as required, and the specific arrangement may be in the conventional manner, as described in CN203878113U and the like.
In the present invention, the hydrogenation apparatus or the pre-hydrogenation apparatus preferably uses a noble metal catalyst, which generally uses Pt and/or Pt as an active component, and the carrier is generally alumina. The feeding mode of the hydrogenation device can be upper feeding or lower feeding.
In the present invention, the hydrogenation unit may comprise more than two catalyst beds. Preferably, the catalyst further comprises a feed line for supplementing any source of hydrogen between the two or more catalyst beds.
In the invention, the supplementing hydrogen can be a proper amount of high-purity hydrogen obtained by reforming the re-contactor, and can also be hydrogen from other sources.
In the present invention, the gas-liquid mixer may be a static mixer or a dynamic mixer, preferably a static mixer. The static mixer can be selected from one or more of SV type static mixer, SK type static mixer, SX type static mixer, SH type static mixer and SL type static mixer, and the dynamic mixer can be selected from one or more of mixing pump, supercritical mixer and stirring mixer.
In the present invention, a catalytic reforming reaction product gas-liquid separator may be further included in which the catalytic reforming reaction product is separated into a hydrogen-rich gas and a reforming reaction liquid-phase product. The gas-liquid separator includes a feed line for feeding the catalytic reforming reaction product to the gas-liquid separator, a line for removing hydrogen-rich gas, a booster compressor for boosting the hydrogen-rich gas, a line for removing the reforming reaction liquid phase product, and a pump for boosting the reforming reaction liquid phase product. Wherein a cooler is generally provided on a feed line for feeding the catalytic reforming reaction product to the gas-liquid separator for cooling the catalytic reforming reaction product.
In the reforming re-contactor, a cooler is usually arranged on a feed line for feeding the pressurized hydrogen-rich gas and the pressurized reforming reaction liquid phase product to the re-contactor, so that the temperature of mixed feed is further reduced, a better light hydrocarbon recovery effect is achieved, and the purity of hydrogen is improved.
In the present invention, a temperature raising means may also be generally provided on the feed line for feeding the mixture from the gas-liquid mixer to the hydrogenation reactor, so that the mixed feed of hydrogen and the bottoms of the re-contactor is heated to the inlet temperature of the hydrogenation reactor by the temperature raising means. Alternatively, a heating device can be arranged on a feed line for feeding hydrogen from any source and the bottom oil of the reforming re-contactor to the gas-liquid mixer, and the heating device is used for preheating the hydrogen and the bottom oil to the inlet temperature of the reactor and then feeding the preheated hydrogen and the bottom oil into the gas-liquid mixer for hydrogen dissolution. The heating device can be a heat exchanger or a heating furnace, and is preferably a heat exchanger.
In the invention, a hydrogenation device reaction product gas-liquid separator can be arranged, and separated gas phase and liquid phase are respectively introduced into a light component removing tower from proper positions.
In the present invention, the operating temperature of the pre-hydrogenation unit is generally less than 10 to 100 ℃ of the hydrogenation unit.
Compared with the prior art, the invention has the following beneficial effects:
1. the hydrogenation system can carry out deep selective hydrogenation on the reforming reaction liquid phase product under a mild process condition so as to remove hydrocarbons containing carbon-carbon double bonds and/or carbon-carbon triple bonds, and the loss of aromatic hydrocarbon in the hydrogenation process can be controlled below 0.5 percent, so that the reforming reaction liquid phase product after hydrogenation can completely meet the quality requirement of a downstream aromatic hydrocarbon extraction device on feeding.
2. Because the hydrogenation reactor is arranged between the re-contactor and the stabilizer, a proper amount of hydrogen obtained by the re-contactor can be directly utilized as a hydrogen source to carry out hydrogenation under the condition of liquid phase hydrogenation, thereby omitting a circulating hydrogen compressor in the existing hydrogenation system and reducing investment cost and operation cost.
3. Because the hydrogenation reactor is arranged between the re-contactor and the stabilizer, the raw material temperature rising and reducing process is reduced, so that the low-temperature heat source of the device can be fully utilized, and the operation energy consumption of the device is reduced.
4. The reaction environment in the hydrogenation reactor is mainly liquid phase reaction, so that the occurrence probability of bias flow and channeling is reduced, and the property of the reforming reaction liquid phase product obtained by refining the device is more stable.
5. Because the hydrogen in the separator of the device is in an unsaturated state, the hydrogen loss or the hydrogen recovery consumption of enterprises is reduced, and the energy consumption of the device is also reduced.
6. The combination of the pre-hydrogenation device and the hydrogenation device can fully utilize the low-temperature activity and the high-temperature activity of the hydrogenation catalyst, thereby being beneficial to prolonging the service life of the catalyst.
7. Through the coupling relation between the hydrogenation device and the light component removing tower, the influence on the operation of the light component removing tower is less when the hydrogenation device adjusts the temperature in a larger range. The hydrogenation device reaction product firstly carries out heat exchange flow of temperature reduction and then temperature rising, and although the heat utilization efficiency is reduced in theory, the inlet temperature fluctuation of the light component removal tower can be ensured to be smaller. The calculation shows that when the reaction temperature of the hydrogenation device is adjusted within the range of 100-230 ℃, the fluctuation range of the inlet temperature of the light component removal tower is about 5 ℃, and the light component removal tower is slowly fluctuated for a long period, and the normal operation of the light component removal tower is not influenced by the simple adjustment of the light component removal tower. The operation of the light component removing tower is not influenced by the adjustment of the temperature of the reactor. The material temperature regulation and control system is arranged before the heavy components at the bottom of the light component removal tower are discharged to the next processing unit (or in the next processing unit), so that the requirement of the next processing unit on the material temperature is met, and the system and the downstream processing unit can automatically and stably operate without excessive manual regulation.
8. The light hydrocarbon in the reforming process is recovered in the device without additionally arranging a light hydrocarbon recovery device.
Drawings
FIG. 1 is a schematic diagram of a construction of the present invention.
Fig. 2 is a schematic diagram of another embodiment of the present invention.
Detailed Description
The reforming reaction liquid-phase product hydrogenation system of the present invention will be described in detail with reference to the accompanying drawings and specific examples.
As shown in fig. 1, the present invention includes: a reforming re-contactor 12 comprising a feed line 9 for feeding pressurized hydrogen-rich gas to the re-contactor and a feed line 8 for feeding pressurized reforming reaction liquid phase product to the re-contactor, a hydrogen removal line 13 for removing hydrogen and a removal line 14 for removing re-contactor produced oil.
In the reforming re-contactor 12, a cooler 11 is further disposed on the feeding line 9 for feeding the pressurized hydrogen-rich gas to the re-contactor, and a cooler 10 may be further disposed on the feeding line 8 for feeding the pressurized reforming reaction liquid-phase product to the re-contactor, so as to further reduce the temperature of the feeding, thereby obtaining better light hydrocarbon recovery effect and improving the purity of the hydrogen in the re-contactor.
A gas-liquid mixer 15 comprising a feed line 14 for feeding the bottom oil from the reforming re-contactor to said gas-liquid mixer, a feed line for feeding hydrogen from any source to said gas-liquid mixer. As shown in fig. 1, in the present embodiment, a feed line for feeding hydrogen from any source to the gas-liquid mixer is connected to a hydrogen removal line 13 for removing hydrogen in the reforming re-contactor, i.e., the hydrogen from any source may be a proper amount of high purity hydrogen obtained from the reforming re-contactor. According to the structure of the gas-liquid mixer, hydrogen can be directly introduced into the gas-liquid mixer, or can be mixed with raw materials at other positions and then enter the gas-liquid mixer.
A hydrogenation reactor 18 comprising a feed line 17 for feeding the mixture from the gas-liquid mixer to said hydrogenation reactor and a hydrogenation product removal line 19 for removing hydrogenation products.
The hydrogenation reactor 18 typically includes more than two hydrogenation catalyst beds 24. The hydrogenation system preferably further comprises a make-up hydrogen feed line for making up hydrogen from any source between the two or more catalyst beds. In the present embodiment, a hydrogen supplementing feed line for supplementing hydrogen from an arbitrary source between two or more catalyst beds is connected to a hydrogen removing line 13 for removing hydrogen in the reforming re-contactor, i.e., a proper amount of high purity hydrogen obtained by the reforming re-contactor can be used as hydrogen supplementing.
The hydrogenation reactor 18 is a liquid phase hydrogenation reactor (mainly a liquid phase, and a small part is a gas phase for material gasification), which can be an upper feed reactor or a lower feed reactor, and the lower feed reactor is preferably used in the present invention.
In the hydrogenation reactor 18, a temperature raising device 16.3 is preferably arranged on a feeding line 17 for feeding the mixture from the gas-liquid mixer to the hydrogenation reactor, and is used for heating the mixed feed of hydrogen and the bottom oil of the re-contactor to the inlet temperature of the hydrogenation reactor. Alternatively, a temperature raising means may be provided on a feed line for feeding the hydrogen and the bottom oil from the re-contactor to the gas-liquid mixer as required. The temperature raising device may be a heating furnace, a heat exchanger, an electric heater, a steam heater, a heat conducting oil heater, or other devices capable of raising the feeding temperature in the art.
In the present invention, a gas-liquid separator 3 is further included, which includes a feed line 1 for feeding a catalytic reforming reaction product to the gas-liquid separator 3, a line 4 for removing a hydrogen-rich gas, a booster compressor 5 for boosting the hydrogen-rich gas, a line 6 for removing a reforming reaction liquid-phase product, and a pump 7 for boosting the reforming reaction liquid-phase product. Wherein, a cooler 2 is also arranged on the feeding pipeline 1 for feeding the catalytic reforming reaction product to the gas-liquid separator 3, and is used for cooling the catalytic reforming reaction product.
In the present invention, a light ends column 20 (also referred to as a stabilizer column) includes a feed line 19 for feeding the liquid phase hydrogenation reactor hydrogenation product to the light ends column, which feed line simultaneously serves as a hydrogenation product take-off line for the hydrogenation reactor 18, an overhead product take-off line 21 for taking off the light ends column overhead gas product, and a take-off line 22 for withdrawing the reforming reaction liquid phase product from the light ends column.
In the invention, the discharged material of the hydrogenation reactor exchanges heat (cools) with the fed material of the hydrogenation reactor in a heat exchanger 16.1 (a heat exchanger A), exchanges heat (heats) with the discharged material of the bottom of the light component removing tower in a heat exchanger 16.2 (a heat exchanger B), and then enters the light component removing tower for fractionation treatment. The discharging material of the hydrogenation reactor is subjected to temperature reduction and then temperature rise adjustment, so that the requirement of stable feeding temperature of the light component removal tower is well met. If the temperature is not adjusted by cooling, the temperature is directly increased, the feeding temperature of the light component removing tower is increased along with the increase of the temperature of the hydrogenation reactor, and the normal operation of the light component removing tower is finally affected.
Fig. 2 is a schematic diagram of another embodiment of the present invention. The main components are the same as the flow in fig. 1, and will not be described again.
The difference is that a pre-hydrogenation reactor 23 is arranged before the hydrogenation reactor, the pre-hydrogenation reaction is carried out after the temperature of the feed of the pre-hydrogenation reactor 23 is raised by a heat exchanger 16.4, the hot material of the heat exchanger 16.4 can be a proper hot material flow, such as the discharged material at the bottom of the light component removing tower which is subjected to heat exchange (temperature reduction) by the heat exchanger 16.2, and the like.
Referring to fig. 1, one process of the present invention for hydrogenating a reforming reaction liquid phase product is:
the reforming reaction product from the reforming reactor enters a gas-liquid separator 3 for separation after passing through a pipeline 1 and a cooler 2, and hydrogen-rich gas and reforming reaction liquid-phase products are obtained after separation. The hydrogen-rich gas obtained by the gas-liquid separator 3 enters a pressurizing compressor 5 for pressurizing through a pipeline 4, and the obtained reforming reaction liquid phase product enters a pump 7 for pressurizing through a pipeline 6. The pressurized hydrogen-rich gas passes through a pipeline 9 and a cooler 11, and the pressurized reforming reaction liquid phase product passes through a pipeline 8 and a cooler 10 and then respectively enters a reforming re-contactor 12 to further remove light hydrocarbons contained in the hydrogen-rich gas. The high-purity hydrogen obtained by the reforming re-contactor 12 is removed through a hydrogen removal pipeline 13, one path of the high-purity hydrogen is mixed with the bottom oil of the reforming re-contactor through a pipeline 14 and then is heated, a gas-liquid mixer 15 and a pipeline 17 are carried out, or the high-purity hydrogen is heated by the gas-liquid mixer 15 and then enters a hydrogenation reactor 18 through the pipeline 17, and is contacted with a hydrogenation catalyst containing active component platinum to carry out liquid-phase hydrogenation reaction, so that hydrocarbon impurities containing carbon-carbon double bonds and/or carbon-carbon triple bonds in a reforming reaction liquid-phase product are removed; another path of high purity hydrogen from the reforming re-contactor is piped to a recycle hydrogen compressor or exit device, and a third path of hydrogen may be provided to pass through the pipework between more than two hydrogenation catalyst beds 24 of the hydrogenation reactor 18 for use as make-up hydrogen. The hydrogenation reaction product is cooled by a heat exchanger 16.1 through a hydrogenation product removal pipeline 19, then heated by a post heat exchanger 16.2 and enters a stabilizer 20, the obtained gas product is discharged by a tower top product removal pipeline 21, and the obtained reforming reaction liquid phase product with reduced impurity content is discharged by a pipeline 22.
The flow simulation calculation is carried out according to the schematic diagram of fig. 1, when the reaction temperature of the hydrogenation reactor 18 is adjusted from the reaction temperature of the hydrogenation device to be in the range of 150-200 ℃, the inlet temperature of the light component removal tower is gradually increased from 186 ℃ to 190 ℃, and the normal operation of the light component removal tower is not influenced by the simple adjustment of the light component removal tower.
Claims (8)
1. A reformate full distillate liquid phase product hydrogenation unit and light ends removal column coupling system comprising:
a hydrogenation unit comprising a feed line for introducing a hydrogenation unit feed to the hydrogenation unit and a hydrogenation product removal line for removing hydrogenation products; a heating device and a temperature control device are arranged on a feeding pipe line of the hydrogenation device and are used for regulating and controlling the reaction temperature of the hydrogenation device;
a light ends column comprising a feed line for introducing a light ends column feed to the light ends column, and a removal line for removing overhead light ends obtained after fractionation, and a removal line for removing bottom heavy ends obtained after fractionation;
the hydrogenation device is in coupling relation with the light component removing tower and comprises a heat exchanger A arranged on a hydrogenation product removing pipeline, a heat exchanger B arranged on a heavy component removing pipeline at the bottom of the tower, wherein the hydrogenation product removing pipeline is communicated with the heat exchanger A and then is communicated with the heat exchanger B through a pipeline, and finally, the hydrogenation product removing pipeline is communicated with the light component removing tower through a feeding pipeline of the light component removing tower; the cold material of the heat exchanger A is fed into the hydrogenation device, and the hot material of the heat exchanger B is the heavy component at the bottom of the light component removing tower.
2. The system according to claim 1, wherein: the pre-hydrogenation device is arranged in front of the hydrogenation device and operated at a temperature lower than that of the hydrogenation device, and an outlet pipeline of the pre-hydrogenation device is communicated with the heat exchanger A.
3. The system according to claim 2, wherein: the hydrogenation device and/or the pre-hydrogenation device are provided with a hydrogen supplementing pipeline and a hydrogen quantity control device.
4. A system according to claim 3, characterized in that: and a gas-liquid mixer is arranged, and the supplementary hydrogen is supplemented into the feeding of the hydrogenation device through the gas-liquid mixer.
5. The system according to claim 2, wherein: the hydrogenation device or the pre-hydrogenation device uses a noble metal catalyst, the catalyst takes Pt as an active component, and the carrier is alumina.
6. The system according to claim 4, wherein: the gas-liquid mixer is a static mixer or a dynamic mixer.
7. The system according to claim 1, wherein: and arranging a hydrogenation device reaction product gas-liquid separator, and respectively introducing the separated gas phase and liquid phase into a light component removing tower from a proper position.
8. The system according to claim 2, wherein: the operating temperature of the pre-hydrogenation device is lower than the temperature of the hydrogenation device by 10-100 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710306524.7A CN108795491B (en) | 2017-05-04 | 2017-05-04 | Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710306524.7A CN108795491B (en) | 2017-05-04 | 2017-05-04 | Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN108795491A CN108795491A (en) | 2018-11-13 |
| CN108795491B true CN108795491B (en) | 2023-07-28 |
Family
ID=64054441
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710306524.7A Active CN108795491B (en) | 2017-05-04 | 2017-05-04 | Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN108795491B (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103666544A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydro-treating method of reformate |
| CN203878113U (en) * | 2014-05-25 | 2014-10-15 | 中国石油化工股份有限公司 | Reforming reaction liquid-phase product hydrogenation system |
| CN206768033U (en) * | 2017-05-04 | 2017-12-19 | 中国石油化工股份有限公司抚顺石油化工研究院 | Reform full cut liquid product hydrogenation plant and cut light tower coupled system |
-
2017
- 2017-05-04 CN CN201710306524.7A patent/CN108795491B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103666544A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Hydro-treating method of reformate |
| CN203878113U (en) * | 2014-05-25 | 2014-10-15 | 中国石油化工股份有限公司 | Reforming reaction liquid-phase product hydrogenation system |
| CN206768033U (en) * | 2017-05-04 | 2017-12-19 | 中国石油化工股份有限公司抚顺石油化工研究院 | Reform full cut liquid product hydrogenation plant and cut light tower coupled system |
Non-Patent Citations (1)
| Title |
|---|
| 谢洪波.1.2Mt/a连续重整装置的节能技改.化工生产与技术.2009,第58-62页. * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108795491A (en) | 2018-11-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN203878113U (en) | Reforming reaction liquid-phase product hydrogenation system | |
| CN100371423C (en) | Hydrocarbons hydrocracking method | |
| JP5937234B2 (en) | Catalytic reforming process and catalytic reforming system for producing gasoline with reduced benzene content | |
| CN103396833B (en) | A kind of synthetic naphtha produces the method for motor spirit | |
| US10829700B2 (en) | Method for the selective hydrogenation of a pyrolysis gasoline feedstock with a three-phase reactor | |
| CN107207976A (en) | For reforming integrated approach and system with isomerization hydrocarbon | |
| KR950003423A (en) | Purification method and apparatus | |
| CN108795491B (en) | Coupling system of reforming full fraction liquid phase product hydrogenation device and light component removing tower | |
| CN108795486B (en) | Coupling system of reforming generated oil liquid phase hydrogenation device and light component removing tower | |
| CN108795490B (en) | Coupling system of hydrogenation device and light component removal tower for reforming full distillate generated oil | |
| CN108795494B (en) | Coupling system of hydrogenation device and light component removing tower for reforming generated oil | |
| CN115537231B (en) | Method for realizing oil reduction and oil increase by changing material flow direction | |
| CN107304371B (en) | A kind of recapitalization generating oil hydrogenation processing method | |
| CN103492533A (en) | High temperature reforming process | |
| CN206768035U (en) | Recapitalization generating oil hydrogenation device and cut light tower coupled system | |
| CN206768029U (en) | Reformed oil liquid-phase hydrogenatin device and cut light tower coupled system | |
| CN206768033U (en) | Reform full cut liquid product hydrogenation plant and cut light tower coupled system | |
| CN206768032U (en) | Reform full cut and generate oily hydrogenation plant and cut light tower coupled system | |
| CN109722297B (en) | Catalytic reforming process system and process method | |
| CN202595054U (en) | Hydrogenation process unit for producing cleaning products | |
| CN107304376B (en) | A kind of reformed oil liquid-phase hydrogenatin processing method | |
| CN109722298B (en) | Energy-saving catalytic reforming process system and process method | |
| CN113122318B (en) | Fluidized bed hydrogenation reaction system and hydrogenation method | |
| CN107304369B (en) | A kind of recapitalization generating oil hydrogenation method | |
| CN107304370A (en) | A kind of recapitalization generating oil hydrogenation process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |