CN110776947A - Catalytic reforming energy-saving system, energy-saving method and catalytic reforming reaction system - Google Patents
Catalytic reforming energy-saving system, energy-saving method and catalytic reforming reaction system Download PDFInfo
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- CN110776947A CN110776947A CN201911117979.XA CN201911117979A CN110776947A CN 110776947 A CN110776947 A CN 110776947A CN 201911117979 A CN201911117979 A CN 201911117979A CN 110776947 A CN110776947 A CN 110776947A
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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
- C10G35/00—Reforming naphtha
- C10G35/04—Catalytic reforming
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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
- C10G35/00—Reforming naphtha
- C10G35/24—Controlling or regulating of reforming operations
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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
- C10G61/00—Treatment of naphtha by at least one reforming process and at least one process of refining in the absence of hydrogen
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1037—Hydrocarbon fractions
- C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
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- 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)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention relates to the technical field of catalytic reforming, and discloses a catalytic reforming energy-saving system, an energy-saving method and a catalytic reforming reaction system. The catalytic reforming energy-saving system comprises a high-pressure absorption tank, a reformed product oil stabilizing tower and a first heat exchanger, wherein the high-pressure absorption tank is communicated with a bottom liquid output pipe, the bottom liquid output pipe is communicated with a feed inlet of the reformed product oil stabilizing tower, the reformed product oil stabilizing tower is communicated with a bottom oil output pipe, the bottom oil output pipe is used as a heat source pipeline, and the bottom liquid output pipe is used as a cold source pipeline and is connected with the first heat exchanger. The catalytic reforming energy-saving method comprises the following steps: and (3) exchanging heat for the bottom liquid generated by the high-pressure absorption tank by using the bottom oil generated by the reformed oil stabilizing tower as a heat source. The catalytic reforming reaction system comprises the catalytic reforming energy-saving system. The catalytic reforming energy-saving system, the catalytic reforming energy-saving method and the catalytic reforming reaction system provided by the invention can reduce the system load, reduce the system energy consumption and realize resource saving.
Description
Technical Field
The invention relates to the technical field of catalytic reforming, in particular to a catalytic reforming energy-saving system, an energy-saving method and a catalytic reforming reaction system.
Background
The reforming device used as a naphtha processing unit mainly takes naphtha as a raw material to produce reformed oil rich in aromatic hydrocarbon, which is used as an aromatic hydrocarbon raw material and a gasoline blending component and is rich in hydrogen and a small amount of liquefied gas. Generally, the method mainly comprises three units of raw material pretreatment, reforming reaction and catalyst regeneration. The pretreatment unit comprises three parts of prefractionation, prehydrogenation and steam stripping, naphtha raw materials from a naphtha stabilizing system enter a prefractionation tower for fractionation, oil gas at the top of the tower is 80-100 ℃, one part of the oil gas is condensed and cooled by an air cooler and a water cooler at the top of the tower and is used as reflux at the top of the tower, and the other part of the oil gas is sent to an n-isopentane separation tower; the method comprises the steps of enabling depentanized oil at the bottom of a prefractionating tower to enter a prehydrogenation reactor after being subjected to pressure boosting, heat exchange and heating temperature rise by a prehydrogenation heating furnace, enabling a reaction product to enter a prehydrogenation reaction feed and a bottom liquid phase of a prehydrogenation liquid separation tank for heat exchange, then entering a prehydrogenation product air cooler and a prehydrogenation product water cooler for condensation and cooling, enabling a hydrogen-rich liquid separation tank to realize gas-liquid separation, enabling a hydrogen-rich liquid phase to circulate back to the prehydrogenation reactor, enabling a bottom liquid phase of the tank to exchange heat with the.
The reforming reaction unit mainly comprises a reforming reaction part, a hydrogen purification part, a reforming fractionation part and the like, refined oil from a pretreatment unit is mixed with reforming circulating hydrogen in a certain hydrogen-oil ratio, and then sequentially passes through a reforming feed heat exchanger, a first reforming heating furnace, a first reforming reactor, a second reforming heating furnace, a second reforming reactor, a third reforming heating furnace, a third reforming reactor, a fourth reforming heating furnace and a fourth reforming reactor, then exchanges heat with the refined oil feed to 100-120 ℃, enters a reforming product water cooler after being cooled to 50-70 ℃ by a reforming product air cooler, realizes the separation of hydrogen and crude gasoline by a low-pressure gas-liquid separation tank and a high-pressure absorption tank, hydrogen enters a hydrogen purification system, crude gasoline (25-40 ℃) at the bottom of the high-pressure absorption tank exchanges heat with bottom oil of a reforming product oil stabilization tower, and then enters a reforming product oil stabilization tower to obtain a qualified stabilized gasoline outlet device, the heat required by the bottom of the reformate stabilizing tower is provided by a heating furnace.
The temperature of oil gas at the top of the prefractionation tower of the reforming device is high, the oil gas is condensed and cooled by an air cooler and a water cooler and then is used as tower top reflux and n-isopentane separation tower feeding, and low-temperature heat is not recovered; the reformed product after heat exchange by the reforming feed heat exchanger has abundant low-temperature heat source; the liquid phase cold energy at the bottom of the high-pressure absorption tank is not fully utilized, and directly exchanges heat with the reformed oil stabilizing tower bottom oil, the heat exchange temperature difference is large, and the feeding temperature of the reformed oil stabilizing tower is lower.
In view of this, the invention is particularly proposed.
Disclosure of Invention
The invention aims to provide a catalytic reforming energy-saving system, a catalytic reforming energy-saving method and a catalytic reforming reaction system.
The invention is realized by the following steps:
in a first aspect, an embodiment provides a catalytic reforming energy-saving system, which includes a high-pressure absorption tank, a reformate stabilizer and a first heat exchanger.
The high-pressure absorption tank is communicated with a bottom liquid output pipe, the reformed product oil stabilizing tower is communicated with a bottom oil output pipe, the bottom oil output pipe is used as a heat source pipeline to be communicated with a heat flow channel of the first heat exchanger, the bottom liquid output pipe is used as a cold source pipeline to be communicated with a cold flow channel of the first heat exchanger, and the bottom liquid output pipe is communicated with a feed inlet of the reformed product oil stabilizing tower and is used for conveying bottom liquid to the reformed product oil stabilizing tower.
In an optional embodiment, the catalytic reforming energy-saving system further comprises a second heat exchanger and a pre-fractionation discharge pipe communicated with the top of a pre-fractionation tower in a pretreatment unit of the catalytic reforming reaction system, the pre-fractionation discharge pipe is used as a heat source pipeline and communicated with a heat flow channel of the second heat exchanger, and a bottom liquid output pipe is used as a cold source pipeline and communicated with a cold flow channel of the second heat exchanger.
In an alternative embodiment the second heat exchanger is located upstream of the first heat exchanger.
In an optional embodiment, the catalytic reforming energy-saving system further includes a second heat exchanger and a reformate output pipe communicated with a reforming reaction unit of the catalytic reforming reaction system, the reformate output pipe is used as a heat source pipeline to be communicated with a heat flow channel of the second heat exchanger, and the base liquid output pipe is used as a cold source pipeline to be communicated with a cold flow channel of the second heat exchanger.
In an optional embodiment, the catalytic reforming energy-saving system further comprises a reforming feed heat exchanger and a reforming raw material inlet pipe communicated with the reforming pretreatment unit, the reforming raw material inlet pipe is used as a cold source pipeline and communicated with a cold flow channel of the reforming feed heat exchanger, the reformate output pipe is used as a heat source pipeline and communicated with a hot flow channel of the reforming feed heat exchanger, and the reforming feed heat exchanger is arranged at the upstream of the second heat exchanger.
In an optional embodiment, the catalytic reforming energy-saving system further comprises a heating furnace at the bottom of the stabilization tower, the reformate stabilization tower is further communicated with a bottom oil return pipe, one end of the bottom oil return pipe is connected with the bottom of the reformate stabilization tower, the other end of the bottom oil return pipe is connected with the lower part of the reformate stabilization tower, and the middle part of the bottom oil return pipe is connected with the heating furnace at the bottom of the stabilization tower.
In a second aspect, an embodiment provides a catalytic reforming energy-saving method, including:
and (3) exchanging heat for the bottom liquid generated by the high-pressure absorption tank by using the bottom oil generated by the reformed oil stabilizing tower as a heat source so as to enable the temperature of the bottom liquid generated by the high-pressure absorption tank to be increased and then enter the reformed oil stabilizing tower.
In an alternative embodiment, before the bottom liquid produced by the high-pressure absorption tank enters the reformate stabilizing tower, the method further comprises the step of exchanging heat for the bottom liquid produced by the high-pressure absorption tank by using a pre-fractionation product produced at the top of a pre-fractionation tower in a pretreatment unit of the catalytic reforming reaction system as a heat source.
In an alternative embodiment, before the bottom liquid produced by the high-pressure absorption tank enters the reformate stabilizing tower, the method further comprises the step of exchanging heat for the bottom liquid produced by the high-pressure absorption tank by using a reformate produced by a reforming reaction unit of the catalytic reforming reaction system as a heat source.
In a third aspect, embodiments provide a catalytic reforming reaction system, including the catalytic reforming energy-saving system.
The invention has the following beneficial effects:
according to the catalytic reforming energy-saving system obtained through the design, due to the specific arrangement of the bottom liquid output pipe, the bottom oil output pipe and the first heat exchanger, the heat exchange between the bottom oil and the bottom liquid can be realized, the temperature of the bottom liquid entering the reformed oil stabilizing tower is increased, the energy supply of the reformed oil stabilizing tower is reduced, the temperature of the bottom oil entering the arene removing device is reduced, and the cooling load of the arene removing device is reduced.
According to the catalytic reforming energy-saving method obtained through the design, the bottom oil generated by the reformed oil stabilizing tower is used as a heat source to exchange heat with the bottom liquid generated by the high-pressure absorption tank. The temperature of the bottom liquid entering the reformed oil stabilizing tower is increased, the energy supply of the reformed oil stabilizing tower is reduced, the temperature of the bottom oil entering the aromatics removal device is reduced, and the cooling load of the aromatics removal device is reduced.
The catalytic reforming energy-saving system comprises the catalytic reforming energy-saving system, so that the reaction system has smaller load and lower energy consumption compared with the conventional catalytic reforming reaction system.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings needed to be used in the embodiments will be briefly described below, it should be understood that the following drawings only illustrate some embodiments of the present invention and therefore should not be considered as limiting the scope, and for those skilled in the art, other related drawings can be obtained according to the drawings without inventive efforts.
FIG. 1 is a process flow diagram of a catalytic reforming energy-saving system provided in example 1 of the present invention;
fig. 2 is a process flow diagram of the catalytic reforming energy-saving system provided in embodiment 2 of the present invention.
Icon: 100 a-catalytic reforming energy-saving system; 100 b-catalytic reforming energy-saving system; 110-a high pressure absorption tank; 111-a base liquid output pipe; 120-a first heat exchanger; 130 a-a second heat exchanger; 130 b-a second heat exchanger; 140-reformate stabilizer column; 141-bottom oil output pipe; 151-pre-fractionation discharge pipe; 2-a prefractionator; 160-stable tower bottom heating furnace; 162-bottom oil return line; 170-reformate outlet pipe; 180-reforming feed heat exchanger; 191-reforming raw material inlet pipe.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings of the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all embodiments of the present invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention. Thus, the following detailed description of the embodiments of the present invention, presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. All other embodiments, which can be obtained by a person skilled in the art without any inventive step based on the embodiments of the present invention, are within the scope of the present invention.
In the description of the present invention, it is to be understood that the terms "center", "longitudinal", "lateral", "length", "width", "thickness", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", "clockwise", "counterclockwise", and the like, indicate orientations and positional relationships based on those shown in the drawings, and are used only for convenience of description and simplicity of description, and do not indicate or imply that the equipment or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be considered as limiting the present invention.
Furthermore, the terms "first", "second" and "first" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include one or more of that feature. In the description of the present invention, "a plurality" means two or more unless specifically defined otherwise.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," "secured," and the like are to be construed broadly and can, for example, be fixedly connected, detachably connected, or integrally formed; can be mechanically or electrically connected; either directly or indirectly through intervening media, either internally or in any other relationship. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the present invention, unless otherwise expressly stated or limited, "above" or "below" a first feature means that the first and second features are in direct contact, or that the first and second features are not in direct contact but are in contact with each other via another feature therebetween. Also, the first feature being "on," "above" and "over" the second feature includes the first feature being directly on and obliquely above the second feature, or merely indicating that the first feature is at a higher level than the second feature. A first feature being "under," "below," and "beneath" a second feature includes the first feature being directly under and obliquely below the second feature, or simply meaning that the first feature is at a lesser elevation than the second feature.
The following describes the catalytic reforming energy-saving system, method and catalytic reforming reaction system provided by the embodiment of the present invention.
According to the general characteristics of the catalytic reforming reaction system comprising a pretreatment unit and a reforming reaction unit at present, in order to reduce the cooling load of an air cooler at the top of a prefractionation tower or an air cooler of a reformate, the cold energy of the bottom liquid phase of a high-pressure absorption tank is utilized to exchange heat with low-temperature oil gas, the feeding temperature of a reforming oil production stabilizing tower is increased, and the temperature of stable gasoline entering a downstream device is controlled by adjusting the temperature after the bottom liquid phase of the high-pressure absorption tank exchanges heat with the low-temperature oil gas, so that the air cooling load and the load of a heating furnace of.
Example 1
As shown in fig. 1, the catalytic reforming economizer system 100a provided in this embodiment includes a high-pressure absorption tank 110, a reformate stabilizer 140, and a first heat exchanger 120.
Specifically, the high-pressure absorption tank 110 is communicated with a bottom liquid output pipe 111, the reformed product oil stabilization tower 140 is communicated with a bottom oil output pipe 141, the bottom oil output pipe 141 serves as a heat source pipeline and is communicated with a heat flow channel of the first heat exchanger 120, the bottom liquid output pipe 111 serves as a cold source pipeline and is communicated with a cold flow channel of the first heat exchanger 120, and the bottom liquid output pipe 111 is communicated with a feed inlet of the reformed product oil stabilization tower 140 and is used for conveying bottom liquid to the reformed product oil stabilization tower.
Most of the gas at the top of the low-pressure gas-liquid separation tank enters a reforming circulating hydrogen compressor for recycling, and a small part of hydrogen-rich gas enters a reforming hydrogen supercharger through an inlet liquid separation tank, is subjected to two-stage pressure boosting and then is mixed with reformed oil from a booster pump at the bottom of the low-pressure gas-liquid separation tank, and enters a high-pressure absorption tank for contacting again. The gas-liquid equilibrium is reached again to improve the purity of the reformed hydrogen. Purified H
2The (high-purity hydrogen) is discharged from the top of the high-pressure absorption tank 110, wherein a small part of the (high-purity hydrogen) is supplied to a device for self use, and a large part of the (high-purity hydrogen) is dechlorinated by the dechlorination tank and then is sent to a hydrogen pipe network. The pressure of the high-pressure absorption tank is 3.5-4.5 MPa, and the temperature is 25-45 ℃.
The bottom liquid of the high-pressure absorption tank 110 enters the reformate stabilizing tower after heat exchange by the first heat exchanger 120. Condensing and cooling the gas phase at the top of the stable tower of the reformed oil through an air cooler and a water cooler, then feeding the gas phase at the top of the stable tower of the reformed oil into a tower top reflux tank, and feeding the gas phase at the top of the tower top reflux tank into a gas pipe network in the device, or feeding the gas phase into a catalytic device to recover liquefied gas components in the device, or feeding the gas phase into a reforming reaction system to reduce the purity of; one part of the liquid phase at the bottom of the tank is returned to the top of the tower through a reflux pump for reflux, and the other part of the liquid phase is taken as sulfur-free liquefied gas and sent out of the device.
The temperature of the bottom oil discharged from the bottom of the reformed oil stabilizer 140 is high, the bottom oil is directly introduced into the aromatics removal device, so that the heat contained in the bottom oil is wasted, and the cooling load of the system is increased, the bottom oil output pipe 141 is used as a heat source pipeline and is connected with the bottom liquid output pipe 111 on the same heat exchanger, the heat of the bottom oil is transferred to the bottom liquid, so that the temperature of the bottom liquid is increased, namely, the feeding temperature of the bottom liquid of the high-pressure absorption tank 110 entering the reformed oil stabilizer 140 is increased, and after the feeding temperature is increased, the energy supplied by the reformed oil stabilizer 140 is reduced. The high temperature of the bottom oil of the reformate stabilizing tower 140 is fully utilized to heat the bottom liquid, so that resource conservation can be well realized, and the cooling load of the system is reduced.
Further, the catalytic reforming energy-saving system 100a further includes a second heat exchanger 130a and a pre-fractionation discharge pipe 151 communicated with the top of the pre-fractionation tower 2 in the pretreatment unit of the catalytic reforming reaction system, the pre-fractionation discharge pipe 151 is used as a heat source pipeline and communicated with a heat flow channel of the second heat exchanger 130a, and the bottom liquid output pipe 111 is used as a cold source pipeline and communicated with a cold flow channel of the second heat exchanger 130 a.
The feed of the prefractionation tower comes from a naphtha stabilizing system (the feed temperature is 80-110 ℃, the temperature of the oil at the top of the tower is 80-100 ℃, and the temperature of the oil at the bottom of the tower is 140-160 ℃), the temperature of the oil gas at the top of the tower is higher, the oil gas at the top of the tower is communicated to an air cooler at the top of the depractionation tower for cooling after the oil gas at the top of the tower is discharged, the temperature of the bottom liquid entering the reforming oil generating stabilizing tower 140 can be increased, the temperature of the oil gas at the top of the prefractionation tower can be reduced, and the cooling load of the air cooler at the top of the fractionation tower is reduced by taking the oil gas at the top of the prefractionat.
In the present embodiment, the second heat exchanger 130a is located upstream of the first heat exchanger 120, i.e., it is closer to the high-pressure absorption tank 110 with respect to the first heat exchanger 120. Namely, the bottom liquid exchanges heat with the oil gas at the top of the prefractionating tower 2, and then exchanges heat with the bottom oil discharged from the bottom of the reformed oil stabilizing tower 140.
The catalytic reforming energy-saving system 100a further comprises a stabilizing tower bottom heating furnace 160, the reformate stabilizing tower 140 is further communicated with a bottom oil return pipe 162, one end of the bottom oil return pipe 162 is connected with the bottom of the reformate stabilizing tower 140, the other end of the bottom oil return pipe 162 is connected with the lower part of the reformate stabilizing tower 140, and the middle part of the bottom oil return pipe 162 is connected with the stabilizing tower bottom heating furnace 160.
The refluxed bottom oil is heated by a stabilizer bottom heating furnace 160 to supply the required heat to the reformate stabilizer 140. The bottom liquid is subjected to heat exchange twice before entering the reformate stabilizing tower 140, so that the temperature of the bottom liquid is increased, and the energy supply of the stabilizing tower bottom heating furnace 160 is reduced.
Exchanging heat between the bottom liquid (25-40 ℃) of the high-pressure absorption tank 110 and oil gas (80-100 ℃) at the top of the prefractionator 2 to 50-70 ℃, then exchanging heat between the bottom liquid and reformed oil stabilizing tower bottom oil (210-230 ℃), and entering the reformed oil stabilizing tower after the heat exchange is 160-200 ℃; and (3) exchanging heat between oil gas at the top of the prefractionation tower and bottom liquid (25-45 ℃) of a high-pressure absorption tank to 60-80 ℃, cooling and condensing the oil gas by an air cooler and a water cooler at the top of the prefractionation tower, wherein one part of the oil gas is used as reflux, and the other part of the oil gas is used as feed of an n-isopentane separation tower.
Examples 1 to 1
In this embodiment, the catalytic reforming economizer system 100a provided in embodiment 1 is implemented as a reforming energy utilization device.
The energy-saving and consumption-reducing process and method of the device are illustrated by taking a 70 ten thousand ton/year continuous reforming device of a certain refinery as an example. The plant uses the first-generation french IFP patented technology for the purpose of producing high octane gasoline components and supplying the feedstock to an aromatics complex.
As shown in fig. 1, the energy saving method for catalytic reforming described in this embodiment specifically includes:
the bottom liquid (40 ℃) from the high-pressure absorption tank 110 and the top oil gas of the prefractionation tower 2 exchange heat to 65 ℃ through a newly added second heat exchanger 130a, then exchange heat to 175 ℃ through a first heat exchanger 120, and then enter a reformed formation oil stabilizing tower 140, and part of the bottom oil of the reformed formation oil stabilizing tower 140 exchanges heat to 90 ℃ through the first heat exchanger 120 and enters a downstream aromatic extraction device. The oil gas (95 ℃) at the top of the prefractionation tower and the bottom liquid (40 ℃) of the high-pressure absorption tank are subjected to heat exchange through a second heat exchanger 130a and then cooled to 78 ℃, enter an air cooler at the top of the prefractionation tower and are cooled to 50 ℃, and are condensed and cooled to 40 ℃ through a water cooler at the top of the prefractionation tower to be used as the top reflux and the feed of an n-isopentane separation tower.
Example 2
As shown in fig. 2, the implementation principle and the resulting technical effect of the catalytic reforming energy saving system 100b provided by the embodiment of the present invention are the same as those of embodiment 1, and for a brief description, reference may be made to the corresponding contents in embodiment 1 where this embodiment is not mentioned.
The catalytic reforming energy-saving system 100b provided by this embodiment includes a second heat exchanger 130b and a reformate output pipe 170 communicated with a reforming reaction unit of the catalytic reforming reaction system, the reformate output pipe 170 is used as a heat source pipeline to be communicated with a heat flow channel of the second heat exchanger 130a, and the base liquid output pipe 111 is used as a cold source pipeline to be communicated with a cold flow channel of the second heat exchanger 130 b.
The temperature of the base solution is increased, the temperature of the reformate is reduced, the reformate needs to be cooled by a reformate air cooler, the temperature of the reformate is reduced by the base solution, the cooling load of the reformate air cooler can be reduced, and the temperature of the base solution can also be increased.
Further, the catalytic reforming energy-saving system 100b further includes a reforming feed heat exchanger 180 and a reforming raw material inlet pipe 191 communicated with the reforming pretreatment unit, the reforming raw material inlet pipe 191 is used as a cold source pipeline to be communicated with a cold flow channel of the reforming feed heat exchanger 180, the reformate output pipe 170 is used as a heat source pipeline to be communicated with a hot flow channel of the reforming feed heat exchanger 180, and the reforming feed heat exchanger 180 is disposed upstream of the second heat exchanger 130 b.
The reformate output pipe 170 also exchanges heat with the reforming raw material before exchanging heat with the base solution, so that the temperature of the reforming raw material is increased, and the energy consumption of the reforming reaction unit is saved.
After being mixed with reforming circulating hydrogen in a certain hydrogen-oil ratio, the refined oil from the reforming pretreatment unit sequentially passes through a reforming feed heat exchanger 180, a first reforming heating furnace, a first reforming reactor, a second reforming heating furnace, a second reforming reactor, a third reforming heating furnace, a third reforming reactor, a fourth reforming heating furnace and a fourth reforming reactor outside the catalytic reforming energy-saving system 100b, then exchanges heat with the refined oil feed to 100-120 ℃, is cooled to 50-70 ℃ by a reformed product air cooler, enters a reformed product water cooler, and then passes through a low-pressure gas-liquid separation tank to realize gas-liquid separation.
The method comprises the following steps of (1) exchanging heat between a base solution (25-40 ℃) of a high-pressure absorption tank 110 and a reformed product (100-120 ℃) from a reforming feed heat exchanger after heat exchange to 50-70 ℃, then exchanging heat between the base solution and bottom oil (210-230 ℃) of a reformed oil stabilizing tower, wherein the temperature is 160-200 ℃ after heat exchange, and entering the reformed oil stabilizing tower; the reformed product of a fourth reforming reactor of the reforming pretreatment unit exchanges heat with 100-120 ℃ through a reforming feed heat exchanger 180, exchanges heat with the base solution of the high-pressure absorption tank 110 to 90-110 ℃, and enters a reformed product air cooler to be cooled to 50-70 ℃; and exchanging heat between the bottom oil of the reformed oil stabilizer 140 and the bottom liquid of the high-pressure absorption tank 110 to 75-95 ℃, and feeding the bottom oil and the bottom liquid into a downstream aromatic extraction device.
Example 2-1
In this embodiment, the catalytic reforming economizer system 100b provided in embodiment 2 is implemented as a reforming energy utilization device.
The energy-saving and consumption-reducing process and method of the device are illustrated by taking a 70 ten thousand ton/year continuous reforming device of a certain refinery as an example. The plant uses the first-generation french IFP patented technology for the purpose of producing high octane gasoline components and supplying the feedstock to an aromatics complex.
The energy-saving method for catalytic reforming described in this embodiment specifically includes:
the reformate from the fourth reforming reactor of the reforming pretreatment unit exchanges heat with the reforming feed to 115 ℃ through the reforming feed heat exchanger 180 along the reformate output pipe 170, then enters the newly-added second heat exchanger 130b to exchange heat with the tank bottom liquid (40 ℃) from the high-pressure absorption tank 110 to 107 ℃, enters the reformate air cooler to be cooled to 55 ℃, and is separated from the crude gasoline through the water cooling, low-pressure gas-liquid separation tank and the high-pressure absorption tank. The bottom liquid (40 ℃) of the high-pressure absorption tank 110 exchanges heat with the reformate (115 ℃) from the reforming feed heat exchanger 180 along the bottom liquid output pipe 111 through the second heat exchanger 130b to 65 ℃, exchanges heat with the bottom oil of the reformed oil stabilizing tower 140 through the first heat exchanger 120 to 175 ℃, enters the reformed oil stabilizing tower 140, and the oil gas at the top of the tower is condensed and cooled through an air cooler and a water cooler at the top of the reformed oil stabilizing tower and then is sent out of the device. The reformed oil stabilizing tower bottom oil enters a downstream aromatic extraction device after being subjected to heat exchange by a first heat exchanger 120 to 90 ℃.
Examples of the experiments
And (3) carrying out data statistics on the system load by the methods provided by the embodiment 1-1 and the embodiment 2-1 and the system load by the original process method. The results are shown in tables 1 and 2.
TABLE 1 comparison of examples 1-1 with the original Process
It can be seen from table 1 that the system provided in example 1 of the present invention, and the method provided in example 1-1, can significantly reduce the air cooling load at the top of the prefractionation column and the heating load at the bottom of the reformate stabilizer column.
TABLE 2 comparison of example 2-1 with the original Process
It can be seen from table 2 that the system provided in example 2 of the present invention, the method provided in example 2-1, can significantly reduce the air cooling load of the reforming reaction product and the heating load of the reforming product stabilized column bottom.
As can be seen from tables 1 and 2, the catalytic reforming energy-saving system and the catalytic reforming energy-saving method provided by the present invention can significantly reduce the load of the whole catalytic reforming reaction system, effectively achieve energy saving, and significantly reduce the production cost.
In summary, according to the catalytic reforming energy-saving system provided by the invention, due to the specific arrangement of the bottom liquid output pipe, the bottom oil output pipe and the first heat exchanger, heat exchange between the bottom oil and the bottom liquid can be realized, the temperature of the bottom liquid entering the reformed oil stabilizing tower is increased, the energy supply of the reformed oil stabilizing tower is reduced, the temperature of the bottom oil entering the aromatics removal device is reduced, and the cooling load of the aromatics removal device is reduced.
And furthermore, a second heat exchanger is arranged in front of the first heat exchanger, and the bottom liquid exchanges heat with oil gas discharged from the top of the prefractionation tower or reformed products from a fourth reforming reactor of the reforming pretreatment unit, so that the temperature of the bottom liquid is further increased, the temperature of the oil gas can be reduced to reduce the air cooling load of the air cooler of the fractionating tower, and the temperature of the reformed products can be reduced to reduce the cooling load of the air cooler of the reformed products.
According to the catalytic reforming energy-saving method provided by the invention, the bottom oil generated by the reformed oil stabilizing tower is used as a heat source to exchange heat with the bottom liquid generated by the high-pressure absorption tank. The temperature of the bottom liquid entering the reformed oil stabilizing tower is increased, the energy supply of the reformed oil stabilizing tower is reduced, the temperature of the bottom oil entering the aromatics removal device is reduced, and the cooling load of the aromatics removal device is reduced.
The chemical reforming reaction system provided by the invention comprises the catalytic reforming energy-saving system provided by the invention, so that the reaction system has smaller load and lower energy consumption compared with the traditional catalytic reforming reaction system.
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. A catalytic reforming energy-saving system is characterized by comprising a high-pressure absorption tank, a reformed oil stabilizing tower and a first heat exchanger,
the high-pressure absorption tank is communicated with a bottom liquid output pipe, the reformed product oil stabilizing tower is communicated with a bottom oil output pipe, the bottom oil output pipe is used as a heat source pipeline to be communicated with a heat flow channel of the first heat exchanger, the bottom liquid output pipe is used as a cold source pipeline to be communicated with a cold flow channel of the first heat exchanger, and the bottom liquid output pipe is communicated with a feed inlet of the reformed product oil stabilizing tower and is used for conveying bottom liquid to the reformed product oil stabilizing tower.
2. The catalytic reforming energy-saving system of claim 1, further comprising a second heat exchanger and a pre-fractionation discharge pipe communicated with the top of a pre-fractionation tower in a pretreatment unit of the catalytic reforming reaction system, wherein the pre-fractionation discharge pipe is used as a heat source pipeline and communicated with a heat flow channel of the second heat exchanger, and the bottom liquid output pipe is used as a cold source pipeline and communicated with a cold flow channel of the second heat exchanger.
3. The catalytic reforming economizer system of claim 2 wherein the second heat exchanger is located upstream of the first heat exchanger.
4. The catalytic reforming energy-saving system of claim 1, further comprising a second heat exchanger and a reformate output pipe communicated with a reforming reaction unit of the catalytic reforming reaction system, wherein the reformate output pipe is communicated with a hot flow channel of the second heat exchanger as a heat source pipeline, and the base liquid output pipe is communicated with a cold flow channel of the second heat exchanger as a cold source pipeline.
5. The catalytic reforming energy-saving system of claim 4, further comprising a reforming feed heat exchanger and a reforming feed inlet pipe communicated with the reforming pretreatment unit, wherein the reforming feed inlet pipe is used as a cold source pipeline and communicated with a cold flow channel of the reforming feed heat exchanger, the reformed product outlet pipe is used as a heat source pipeline and communicated with a heat flow channel of the reforming feed heat exchanger, and the reforming feed heat exchanger is arranged at the upstream of the second heat exchanger.
6. The catalytic reforming energy-saving system according to any one of claims 1 to 5, further comprising a heating furnace at the bottom of the stabilizer tower, wherein the reformate stabilizer tower is further communicated with a bottom oil return pipe, one end of the bottom oil return pipe is connected with the bottom of the reformate stabilizer tower, the other end of the bottom oil return pipe is connected with the lower part of the reformate stabilizer tower, and the middle part of the bottom oil return pipe is connected with the heating furnace at the bottom of the stabilizer tower.
7. A catalytic reforming energy-saving method is characterized by comprising the following steps:
and exchanging heat for the bottom liquid generated by the high-pressure absorption tank by using the bottom oil generated by the reformed oil stabilizing tower as a heat source so as to enable the temperature of the bottom liquid generated by the high-pressure absorption tank to be increased and then enter the reformed oil stabilizing tower.
8. The catalytic reforming energy-saving method according to claim 7, further comprising exchanging heat of the bottom liquid produced by the high-pressure absorption tank with a pre-fractionation product produced at the top of a pre-fractionation tower in a pretreatment unit of a catalytic reforming reaction system as a heat source before the bottom liquid produced by the high-pressure absorption tank enters the reformate stabilizing tower.
9. The catalytic reforming energy-saving method according to claim 7, further comprising exchanging heat of the bottom liquid produced by the high-pressure absorption tank with a reformate produced by a reforming reaction unit of a catalytic reforming reaction system as a heat source before the bottom liquid produced by the high-pressure absorption tank enters the reformate stabilizing tower.
10. A catalytic reforming reaction system comprising a catalytic reforming economizer system as claimed in any one of claims 1 to 6.
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