CN111534327B - Reforming pretreatment system, reforming pretreatment method and application - Google Patents
Reforming pretreatment system, reforming pretreatment method and application Download PDFInfo
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- CN111534327B CN111534327B CN202010395364.XA CN202010395364A CN111534327B CN 111534327 B CN111534327 B CN 111534327B CN 202010395364 A CN202010395364 A CN 202010395364A CN 111534327 B CN111534327 B CN 111534327B
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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
- 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
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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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Abstract
The invention discloses a reforming pretreatment system, a reforming pretreatment method and application, and relates to the technical field of catalytic reforming. On the basis of researching the characteristics of the process flow of the reforming pretreatment system and combining the first law and the second law of thermodynamics, the effective energy recycling optimization design of the pretreatment system is carried out. The heat of the pre-hydrogenation reaction product is fully recovered, the naphtha feeding of the pre-fractionating tower is added for heat exchange with the pre-hydrogenation reaction product, the temperature of the depentanized oil at the bottom of the pre-fractionating tower is increased, the bottom oil of the pre-fractionating tower and the pre-hydrogenation feeding heat exchanger are directly subjected to heat exchange and temperature rise, the energy consumption of a heating furnace is saved, and the effective energy loss is reduced.
Description
Technical Field
The invention relates to the technical field of catalytic reforming, in particular to a reforming pretreatment system, a reforming pretreatment method and application.
Background
The reformer pretreatment system is an indispensable component of the reformer as a pretreatment unit of the reforming reaction system. Generally, straight-run naphtha fraction or naphtha from a naphtha stabilizing system is used as a raw material, impurities in light naphtha are removed through prefractionation, pre-hydrogenation and stripping to obtain refined oil, and then reforming reaction is carried out under certain reaction conditions to produce high-octane gasoline components and aromatic hydrocarbons.
The feeding of the prefractionation system mainly comprises straight-run naphtha fraction with the initial boiling point of 175 ℃ or naphtha from a naphtha stabilizing system, the straight-run naphtha fraction and depentanized oil at the bottom of the prefractionation tower exchange heat to 95-135 ℃ through a prefractionation feeding pump, the straight-run naphtha fraction enters a prefractionation tower, one part of a liquid phase stream (topping oil) at the top of the tower is sent back to the top of the prefractionation tower through a prefractionation tower reflux pump to be refluxed, and the other part of the liquid phase stream is sent to an n-isopentane separation tower. The tower bottom depentanized oil exchanges heat with the feeding naphtha of the prefractionating tower, is mixed with the prehydrogenation circulating hydrogen and the reformed supplementary hydrogen through a prehydrogenation feeding pump, and then enters a prehydrogenation reactor for reaction after passing through a prehydrogenation feeding heat exchanger and a prehydrogenation heating furnace, so as to remove the impurities harmful to the reforming reaction catalyst, and the heat required by the kettle of the prefractionating tower is provided by the heating furnace.
The pre-hydrogenation reaction product from the pre-hydrogenation reaction system exchanges heat with the pre-hydrogenation feeding material, then exchanges heat with the liquid from the pre-hydrogenation liquid separation tank through the feeding heat exchanger of the stripping tower, enters the air cooler for the pre-hydrogenation reaction product and the water cooler for the pre-hydrogenation reaction product, and enters the pre-hydrogenation gas-liquid separation tank after being cooled and condensed. Most of hydrogen in the gas phase at the top of the tank is recycled by a pre-hydrogenation circulating compressor, oil at the bottom of the tank is self-pressurized to a feeding heat exchanger of a stripping tower, exchanges heat with a pre-hydrogenation reaction product to 55-80 ℃, then exchanges heat to 180-205 ℃ by the feeding/bottom heat exchanger of the stripping tower, enters the stripping tower, further removes trace water and trace sulfur, refined oil obtained at the bottom of the stripping tower enters a reforming reaction system, and heat required by the kettle of the stripping tower is provided by a heating furnace.
In the reforming device pretreatment system, the heat contained in the pre-hydrogenated reaction product after heat exchange from the pre-hydrogenated feeding heat exchanger is more, and complete heat exchange with the feeding of the stripping tower is not realized; the problems of great efficiency loss and low energy utilization efficiency exist in the heat exchange of the depentanized oil at the bottom of the prefractionation tower and the feeding naphtha of the prefractionation tower.
In view of this, the invention is particularly proposed.
Disclosure of Invention
The present invention is directed to a reforming pretreatment system, a reforming pretreatment method, and an application thereof to solve the above-mentioned problems.
The invention is realized by the following steps:
a reforming pretreatment system comprises a prefractionator, a pre-hydrogenation feed heat exchanger, a pre-hydrogenation reactor, a pre-hydrogenation heating furnace and a prefractionator feed heat exchanger, wherein a bottom oil output pipe is arranged at the bottom of the prefractionator, the bottom oil output pipe is used as a cold source pipeline and communicated with a cold flow pipeline inlet of the pre-hydrogenation feed heat exchanger, a cold flow pipeline outlet of the pre-hydrogenation feed heat exchanger is communicated with the pre-hydrogenation heating furnace, the pre-hydrogenation feed heat exchanger is provided with a heat flow pipeline inlet and a heat flow pipeline outlet, the heat flow pipeline inlet is communicated with the pre-hydrogenation reactor, and an outlet of the heat flow pipeline is communicated with a heat flow inlet of the prefractionator feed heat exchanger and participates in heating and heat exchange of feeding.
The present invention is being studied
On the basis of analysis, namely an effective energy analysis technology, the mass part in the energy transfer and conversion process is recycled as much as possible. By utilizing the heat of the reaction product in the pre-hydrogenation reactor, heat exchange is carried out between the heat of the reaction product and the bottom oil at the bottom of the pre-distillation tower in the pre-hydrogenation feeding heat exchanger, the temperature of the depentanized oil at the bottom of the pre-distillation tower entering a pre-hydrogenation reaction system is increased, and the fuel consumption of a pre-hydrogenation heating furnace is reduced; meanwhile, the loss of the reaction effective energy caused by introducing the depentanized oil at the bottom of the pre-fractionation tower into the pre-hydrogenation reaction system after cooling and heating is avoided, and the depentanized oil at the bottom of the pre-fractionation tower is directly introduced into the pre-hydrogenation feeding heat exchanger to be heated and heated, so that the fuel consumption of the pre-hydrogenation heating furnace is reduced. In addition, the reaction product after heat exchange of the pre-hydrogenation feeding heat exchanger is continuously fed into the feeding heat exchanger of the pre-fractionating tower to carry out feeding temperature rise, so that the heat source consumption of the pre-fractionating tower is reduced, and the energy utilization rate is improved.
Further, in one embodiment, the straight-run naphtha fraction or naphtha from the naphtha stabilizing system is connected with a pre-fractionating tower feeding heat exchanger through a pre-fractionating feeding pump, and enters the pre-fractionating tower after heat exchange and temperature rise; the depentanized oil at the bottom of the pre-distillation tower passes through a pre-hydrogenation feed pump, is mixed with pre-hydrogenation circulating hydrogen and reformed supplementary hydrogen, and then enters a pre-hydrogenation feed heat exchanger for heat exchange and temperature rise.
The naphtha raw material temperature is 75-100 ℃. According to the heat source consumption condition of the prehydrogenation reaction products, the naphtha raw material exchanges heat with the prehydrogenation reaction products in a pre-fractionating tower feeding heat exchanger to raise the temperature, wherein the prehydrogenation reaction products are the prehydrogenation reaction products which are obtained from the prehydrogenation heat exchanger and subjected to heat exchange.
One part of a liquid phase material flow (topping oil) of the distillate at the top of the prefractionator after condensation and cooling is sent back to the top of the prefractionator through a prefractionator reflux pump to be refluxed, and the other part of the liquid phase material flow is sent to an n-isopentane separation tower. The feeding temperature of the pre-fractionating tower is 95-135 ℃.
In a preferred embodiment of the present invention, the reforming pretreatment system further comprises a heat source supply system, a heat source of the heat source supply system is provided by a convection section of the reforming reaction furnace, a bottom oil output pipe at the bottom of the prefractionation tower comprises two branches, one of the two branches is communicated with the convection section of the reforming reaction furnace, and the bottom oil heated from the convection section of the reforming reaction furnace is communicated with the prefractionation tower through a hot oil output pipe; and the other branch of the bottom oil output pipe is communicated with the inlet of a cold flow pipeline of the pre-hydrogenation feeding heat exchanger.
The convection section of the reforming reaction furnace is used for providing heat for the pre-fractionating tower, and the heat supply of the original heating furnace is completely removed, so that high-quality high-use and low-quality low-use are realized.
In addition, in other embodiments, the heat supply of the original heating furnace can be partially reserved according to the requirement of energy supply.
The original heating furnace has high operation cost, the original heating furnace can provide a heat source of 500-165 ℃, the depentanized oil sent out from the bottom of the pre-fractionation tower only needs to be heated to 140-165 ℃, and the heat source waste of the depentanized oil heated by the original heating furnace is high, thereby belonging to high quality and low use. The inventor creatively discovers that the energy consumption can be greatly reduced by adopting the convection section of the reforming reaction furnace as the heat source supply, the load of the heating furnace can be obviously reduced, and the energy-saving effect is obvious. The convection section of the reforming reaction furnace can provide a heat source at the temperature of 240 ℃ and 400 ℃, and the depentanized oil is dragged into the convection chamber of the reforming reaction furnace to be heated, so that the energy consumption is greatly reduced, and the operation cost is saved.
Preferably, the temperature of the convection chamber of the reforming reaction furnace is 240-400 ℃.
And the other branch of the depentanized oil enters the pre-hydrogenation feeding heat exchanger in a liquid phase manner, and exchanges heat with a high-temperature pre-hydrogenation reaction product in the pre-hydrogenation feeding heat exchanger, so that the temperature of the depentanized oil is increased. Therefore, the heat source consumption of the pre-hydrogenation heating furnace can be reduced, and the depentanized oil can enter the pre-hydrogenation reactor for hydrogenation reaction only by consuming a lower heat source. The reforming pretreatment system provided by the invention is beneficial to reducing power consumption and reducing efficiency loss.
The depentanized oil at the bottom of the prefractionation tower can exchange heat with naphtha feed through a prefractionation tower feed heat exchanger, or directly enter a prehydrogenation reaction system without passing through the prefractionation tower feed heat exchanger.
In a preferred embodiment of the application of the present invention, the above-mentioned pre-hydrogenation feeding heat exchanger sequentially connects the pre-hydrogenation heating furnace and the pre-hydrogenation reactor through a pipeline, and a reaction product outlet is arranged at the bottom of the pre-hydrogenation reactor, and the reaction product outlet is communicated with a heat flow pipeline inlet of the pre-hydrogenation feeding heat exchanger through a pipeline.
In a preferred embodiment of the present invention, the reforming pretreatment system further includes a stripper feed heat exchanger, a pre-hydrogenated product air cooler, a pre-hydrogenated product water cooler, and a pre-hydrogenated liquid separation tank, wherein a heat flow inlet of the stripper feed heat exchanger is communicated with a heat flow outlet of the pre-fractionating tower feed heat exchanger, a heat flow outlet of the stripper feed heat exchanger is sequentially communicated with the pre-hydrogenated product air cooler, the pre-hydrogenated product water cooler, and the pre-hydrogenated liquid separation tank through a pipeline, a bottom oil outlet is disposed at the bottom of the pre-hydrogenated liquid separation tank, and the bottom oil outlet is communicated with a cold flow inlet of the stripper feed heat exchanger through a pipeline.
The method comprises the steps of firstly exchanging heat of a pre-hydrogenation reaction product from a pre-hydrogenation reactor with a pre-hydrogenation reaction feed to 120-150 ℃, then exchanging heat of the pre-hydrogenation reaction product through a stripping tower feed heat exchanger, then cooling the pre-hydrogenation reaction product to 30-40 ℃ in a pre-hydrogenation product air cooler and a pre-hydrogenation product water cooler, and then entering a pre-hydrogenation liquid separation tank.
The reaction product after heat exchange between the pre-hydrogenation feeding heat exchanger and the pre-hydrogenation reaction feeding can exchange heat with naphtha raw material through the pre-fractionating tower feeding heat exchanger and then realize complete heat exchange with the liquid at the bottom of the pre-hydrogenation liquid separation tank through the stripping tower feeding heat exchanger. In other embodiments, according to the temperature of the reaction product after heat exchange, the reaction product after heat exchange between the pre-hydrogenation feed heat exchanger and the pre-hydrogenation reaction feed may also directly enter the feed heat exchanger of the stripping tower and the liquid at the bottom of the pre-hydrogenation liquid separation tank to realize complete heat exchange without entering the feed heat exchanger of the pre-distillation tower.
In other embodiments, the hydrogen-containing gas separated from the pre-hydrogenation gas-liquid separation tank is pressurized and circulated by a pre-hydrogenation recycle hydrogen compressor, and a small part of tail hydrogen is discharged into a fuel gas pipe network under the pressure control.
In an embodiment of the invention with a better application, the stripper column feed heat exchanger is further provided with a cold flow outlet, the cold flow outlet of the stripper column feed heat exchanger is communicated with the cold flow inlet of the stripper column bottom heat exchanger through a pipeline, and the cold flow outlet of the stripper column bottom heat exchanger is communicated with the stripper column through a pipeline.
Liquid-phase material flow at the bottom of the pre-hydrogenation liquid separation tank enters a feeding heat exchanger of a stripping tower through hydraulic control self-pressure to realize complete heat exchange with a pre-hydrogenation reaction product to 80-120 ℃, and then enters the stripping tower through heat exchange of a heat exchanger at the bottom of the stripping tower so as to remove trace water and trace sulfur.
Most of liquid phase material flow after the distillate at the top of the stripping tower is condensed and cooled is sent back to the top of the stripping tower as reflux after being boosted by a reflux pump at the top of the stripping tower, and the rest of liquid phase material flow is sent out of a device as sulfur-containing liquefied gas. The feeding temperature of the stripping tower is 180-205 ℃.
In a preferred embodiment of the application of the invention, the bottom of the stripping tower is provided with a refined oil outlet, the refined oil outlet is communicated with a heat flow inlet of a heat exchanger at the bottom of the stripping tower, and the heat flow outlet of the heat exchanger at the bottom of the stripping tower is connected with a reforming reaction system.
In a preferred embodiment of the present invention, the pipeline connected to the refined oil outlet is provided with two branches, one of the two branches is communicated with the stripper kettle heating furnace, the stripper kettle heating furnace is communicated with the stripper through the pipeline, and the other branch is communicated with the heat flow inlet of the stripper bottom heat exchanger.
And (3) carrying out heat exchange on the refined naphtha (refined oil) at the bottom of the stripping tower and the feed of the stripping tower through a heat exchanger at the bottom of the stripping tower to 125-160 ℃, and then entering a reforming reaction system.
In other embodiments the heat required for the stripper bottoms is provided by the convection section of the reforming reactor.
In another embodiment, the heat required for the stripper bottoms is provided in whole or in part by the convection section of the reforming reactor. The temperature of the convection chamber of the reforming reaction furnace is 240-400 ℃.
A reforming treatment system comprises the reforming pretreatment system. The reforming pretreatment system is a pretreatment unit of the reforming reaction system.
A method of reforming pretreatment, comprising: and (2) performing heat exchange and temperature rise on the bottom oil generated by the pre-fractionating tower by using a pre-hydrogenation feeding heat exchanger, then entering a pre-hydrogenation heating furnace for temperature rise, further entering a pre-fractionating tower feeding heat exchanger for temperature rise after heat exchange and temperature reduction of a heat source in the pre-hydrogenation feeding heat exchanger, and introducing the heated feeding into the pre-fractionating tower.
In a preferred embodiment of the application of the present invention, the product obtained after the reaction in the pre-hydrogenation reactor enters a heat flow inlet of a pre-hydrogenation feed heat exchanger, and a heat source is provided for the bottom oil generated by the pre-fractionation tower in the pre-hydrogenation feed heat exchanger to perform heat exchange and temperature rise.
Preferably, the product after the reaction in the pre-hydrogenation reactor is subjected to heat exchange and temperature reduction in a pre-hydrogenation feed heat exchanger, then the product is introduced into a pre-fractionating tower feed heat exchanger and the feed is heated, and the reaction product after the temperature reduction in the pre-hydrogenation reactor is introduced into a stripping tower feed heat exchanger.
According to the reforming pretreatment method provided by the invention, the cooling load of the air cooler of the pre-hydrogenation reaction product is reduced by fully utilizing the heat of the pre-hydrogenation reaction product, the heat exchange between the pre-hydrogenation reaction product and the feeding material of the naphtha of the pre-fractionating tower is newly increased, the temperature of the depentanized oil at the bottom of the pre-fractionating tower entering the pre-hydrogenation reaction system is increased, and the fuel consumption of the pre-hydrogenation heating furnace is reduced. The method strengthens the heat exchange of the feeding heat exchanger of the stripping tower, thereby reducing the heat exchange load of the bottom heat exchanger of the stripping tower and improving the external output energy of the refined oil. The convection section of the reforming reaction furnace is utilized to provide heat for the prefractionator or the stripping tower, and the heat supply of the original heating furnace is partially reserved or completely removed, so that high-quality high-use and low-quality low-use are realized; the method can reduce the effective energy loss of the pretreatment system and improve the energy utilization rate.
The invention has the following beneficial effects:
the invention provides a reforming pretreatment system, a reforming pretreatment method and application, and aims to optimize the effective energy recycling design of the pretreatment system on the basis of researching the characteristics of the process flow of the reforming pretreatment system and combining the first law and the second law of thermodynamics. The heat of the pre-hydrogenation reaction product is fully recovered, the naphtha feeding of the pre-fractionating tower is added for heat exchange with the pre-hydrogenation reaction product, the temperature of the depentanized oil at the bottom of the pre-fractionating tower is increased, the bottom oil of the pre-fractionating tower and the pre-hydrogenation feeding heat exchanger are directly subjected to heat exchange and temperature rise, the energy consumption of a heating furnace is saved, and the effective energy loss is reduced. The reforming pretreatment method provided by the invention is also beneficial to reducing the load of a subsequent prehydrogenation product air cooler and a subsequent water cooler.
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 prior art flow diagram of a reforming pretreatment system as provided in example 1;
FIG. 2 is a flow chart of the reforming pretreatment energy saving system process technology provided in example 2.
200-a reforming pretreatment system; 210-prefractionator feed heat exchanger; 1-a prefractionator; 2-a reboiling furnace at the bottom of the prefractionator; 220-a pre-hydrogenated feed heat exchanger; 3-prehydrogenation heating furnace; 4-a pre-hydrogenation reactor; 230-stripper feed heat exchanger; 240-prehydrogenation product air cooler; 250-a prehydrogenation product water cooler; 260-a pre-hydrogenation liquid separation tank; 270-stripper bottoms heat exchanger; 5-a stripping tower; 6-reboiling furnace in the stripping tower kettle.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions in the embodiments of the present invention will be clearly and completely described below. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer.
The features and properties of the present invention are described in further detail below with reference to examples.
Example 1
This example provides a conventional reforming pretreatment system 200, and as shown in fig. 1, the pretreatment system of 84 ten thousand tons/year continuous reforming raw material in a certain refinery is exemplified by a "fractionation-first followed by hydrogenation" flow scheme. The system comprises a prefractionator feeding heat exchanger 210, a prefractionator 1, a prefractionator kettle reboiling furnace 2, a prehydrogenation feeding heat exchanger 220, a prehydrogenation heating furnace 3, a prehydrogenation reactor 4, a stripping tower feeding heat exchanger 230, a prehydrogenation product air cooler 240, a prehydrogenation product water cooler 250, a prehydrogenation liquid separation tank 260, a stripping tower bottom heat exchanger 270, a stripping tower 5 and a stripping tower kettle reboiling furnace 6.
Referring to fig. 1, a naphtha raw material from a naphtha stabilizing system enters a prefractionator 1 after exchanging heat with depentanized oil at the bottom of the prefractionator through a prefractionator feed heat exchanger 210 and heating to 102 ℃. In this example, the oil temperature of the naphtha feedstock was 90 ℃.
The temperature of the pre-distillation tower kettle is 150 ℃, heat is supplied by a reboiling furnace 2 of the pre-distillation tower kettle, and the heat load is 8536 kW.
The heat-exchanged depentanized oil at the bottom of the pre-distillation tower (oil temperature 136 ℃) is subjected to pressure increase by a pre-hydrogenation feeding pump, then is mixed with circulating hydrogen from a pre-hydrogenation circulating hydrogen compressor and reforming supplementary hydrogen, is subjected to heat exchange and temperature rise with pre-hydrogenation reaction products by a pre-hydrogenation feeding heat exchanger 220, is heated to the reaction temperature by a pre-hydrogenation heating furnace 3, and then enters a pre-hydrogenation reactor 4 for pre-hydrogenation reaction. The heat load of the prehydrogenation furnace 3 was 3194 kW.
The pre-hydrogenation reaction product is led out from the bottom of the pre-hydrogenation reactor 4, exchanges heat with the pre-hydrogenation reaction feed through the pre-hydrogenation feed heat exchanger 220, is cooled to 140 ℃, and then enters the stripping tower feed heat exchanger 230.
The temperature is reduced to 117 ℃ by heat exchange in a feeding heat exchanger 230 of a stripping tower, then the cooled gas enters a prehydrogenation product air cooler 240 to be cooled to 75 ℃, then the cooled gas enters a prehydrogenation product water cooler 250 to be cooled to 40 ℃, and the cooled product enters a prehydrogenation liquid separation tank 260.
The recycle hydrogen separated from the pre-hydrogenation liquid separator 260 is introduced into the pre-hydrogenation reactor. The liquid phase material flow at the bottom of the pre-hydrogenation liquid separation tank 260 is subjected to hydraulic control self-pressure, enters the feeding heat exchanger 230 of the stripping tower, and is subjected to heat exchange with the pre-hydrogenation reaction product to be heated to 68 ℃.
The liquid phase material flow heated to 68 ℃ in the feeding heat exchanger 230 of the stripping tower enters the bottom heat exchanger 270 of the stripping tower to exchange heat to 195 ℃, and then enters the stripping tower 5 to further remove trace water and trace sulfur.
The stripping tower 5 is supplied with heat by a reboiling furnace 6 at the bottom of the stripping tower, the temperature at the bottom of the stripping tower is 227 ℃, and the heat load is 5588 kW. The refined oil at the bottom of the stripping tower exchanges heat with the feed of the stripping tower to 114 ℃ through a heat exchanger 270 at the bottom of the stripping tower and then enters a downstream reforming reaction system.
Example 2
Referring to fig. 2, a reforming pretreatment system 200 according to the present invention is provided, and the pretreatment system of a 84-million ton/year continuous reforming raw material in a certain refinery is taken as an example, and the pretreatment system of the device adopts a flow mode of fractionation before hydrogenation. The system comprises a prefractionator feeding heat exchanger 210, a prefractionator 1, a prefractionator kettle reboiling furnace 2, a prehydrogenation feeding heat exchanger 220, a prehydrogenation heating furnace 3, a prehydrogenation reactor 4, a stripping tower feeding heat exchanger 230, a prehydrogenation product air cooler 240, a prehydrogenation product water cooler 250, a prehydrogenation liquid separation tank 260 and a stripping tower bottom heat exchanger 270.
Referring to fig. 2, a naphtha feedstock from a naphtha stabilization system is passed through a prefractionator feed heat exchanger 210 and a prehydrogenation reaction product (140 ℃) from a prehydrogenation feed heat exchanger 220 to a temperature of 102 ℃ before entering prefractionator 1. In this example, the oil temperature of the naphtha feedstock was 90 ℃.
The depentanized oil at the bottom of the prefractionation tower (150 ℃) directly enters a prehydrogenation feeding heat exchanger 220 through a prehydrogenation feeding pump and exchanges heat with the naphtha feeding of the prefractionation tower without passing through a prefractionation tower feeding heat exchanger 210.
In the embodiment, the heat required by the pre-fractionating tower 1 is completely provided by the convection section of the reforming reaction furnace, the temperature of the convection section of the reforming reaction furnace is 260-400 ℃, and the surplus heat is 13000 kW.
The temperature of the pre-hydrogenated reaction product from the pre-hydrogenation reactor 4 and the pre-hydrogenated feed after heat exchange in the pre-hydrogenated feed heat exchanger 220 is 140 ℃, the pre-hydrogenated reaction product enters the pre-distillation tower feed heat exchanger 210, and enters the stripping tower feed heat exchanger 230 to exchange heat with the bottom oil of the pre-hydrogenated liquid separation tank for cooling after the heat exchange is cooled to 125 ℃.
The cooled material flow enters a pre-hydrogenation product air cooler 240 to be cooled to 55 ℃, and enters a pre-hydrogenation liquid separation tank 260 to realize gas-liquid separation after being cooled to 40 ℃ by a pre-hydrogenation product water cooler 250.
The temperature of the pre-hydrogenated liquid separation tank bottom oil after heat exchange with the pre-hydrogenated reaction product (125 ℃) from the pre-fractionating tower feeding heat exchanger 210 is 95 ℃, and the tank bottom oil after heat exchange enters the stripping tower bottom heat exchanger 270 to exchange heat to 195 ℃ and then enters the stripping tower 5 (not shown in the figure).
The refined oil (135 ℃) at the bottom of the stripping tower after the heat exchange of the bottom heat exchanger 270 of the stripping tower enters a reforming reaction system of a reforming device.
Experimental example 1
The energy consumption and the loss of performance of the process and the apparatus provided in examples 1 and 2 are compared in tables 1 and 2.
Table 1 comparison of heat exchange duty for example 1 and example 2.
| Example 1 | Example 2 | Increase/decrease amount of% | |
| The load of the feed heat exchanger of the pre-fractionating tower,kW | 902.94 | 902.94 | 0.00 |
| load of feed heat exchanger of stripping tower, kW | 1450.42 | 3029.51 | -108.87 |
| Stripper feed/bottom heat exchanger load, kW | 8423.68 | 6641.38 | 21.16 |
| Pre-hydrogenated product air cooler load, kW | 2477.61 | 1092.52 | 55.90 |
| Pre-hydrogenation product water cooler load, kW | 1878.43 | 785.72 | 58.17 |
| kW for reboiler in pre-fractionating tower | 8536.00 | 0.00 | 100.00 |
| Prehydrogenation heating furnaces, kW | 3194.00 | 2291.06 | 28.27 |
Table 2 example 1 and example 2 are compared for loss of effective performance.
As can be seen from table 1, the heat exchange duty of the prefractionator feed heat exchanger 210 was unchanged for example 1 and example 2, i.e., the prefractionator feed conditions were unchanged.
In the embodiment 2, the added pre-hydrogenation reaction product exchanges heat with the feed of the pre-fractionating tower, so that the repeated cooling and heating of the depentanized oil at the bottom of the pre-fractionating tower are avoided, and the heat load of the pre-hydrogenation heating furnace is reduced by 28.27%.
Example 2 complete heat exchange was achieved due to the enhanced heat exchange of the pre-hydrogenated reaction product with the pre-hydrogenated tank bottom liquid, with the load on the stripper feed heat exchanger increased from 1450.42kW to 3029.51kW before and after optimization.
This reduces the heat required to reach 195 c feed temperature in the stripper column feed, thereby reducing 21.16% of the stripper column base exchanger load, and increasing the stripper column base refinery temperature from 114 c to 135 c at this time, while maintaining the feed conditions to the stripper column 5, which reduces the heat required to be supplied to the reforming reaction system.
Example 2 reduced the cooling duty of the pre-hydrogenation reaction system compared to example 1, and the pre-hydrogenated product air cooler and water cooler duty was reduced by 55.90% and 58.17%, respectively.
In addition, in the embodiment 2, the convection section of the reforming reaction furnace is used for supplying heat to the reboiling furnace of the pre-fractionating tower kettle, so that the fuel consumption of one heating furnace is saved.
The effective energy recovery of the pretreatment systems of example 1 and example 2 is shown in Table 2.
The prefractionator feed heat exchanger, stripper bottoms heat exchanger, pre-hydrogenated product air cooler, and pre-hydrogenated product water cooler of example 2 had performance losses that were reduced by 21.81%, 9.13%, 35.02%, 80.69%, and 76.77%, respectively.
From the above test data, the reforming pretreatment system 200 and the reforming pretreatment method provided by the present invention can enhance heat exchange, significantly reduce the energy consumption of the pretreatment system, reduce the efficiency loss of the process, and improve the energy utilization rate.
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 reforming pretreatment system is characterized by comprising a prefractionator, a pre-hydrogenation feed heat exchanger, a pre-hydrogenation reactor, a pre-hydrogenation heating furnace and a prefractionator feed heat exchanger, wherein a bottom oil output pipe is arranged at the bottom of the prefractionator, the bottom oil output pipe is used as a cold source pipeline and communicated with a cold flow pipeline inlet of the pre-hydrogenation feed heat exchanger, a cold flow pipeline outlet of the pre-hydrogenation feed heat exchanger is communicated with the pre-hydrogenation heating furnace, the pre-hydrogenation feed heat exchanger is provided with a heat flow pipeline inlet and a heat flow pipeline outlet, the heat flow pipeline inlet is communicated with the pre-hydrogenation reactor, and an outlet of the heat flow pipeline is communicated with the heat flow inlet of the prefractionator feed heat exchanger and participates in heating heat exchange of feeding;
the reforming pretreatment system also comprises a heat source supply system, wherein a heat source of the heat source supply system is provided by a convection section of the reforming reaction furnace, a bottom oil output pipe at the bottom of the prefractionating tower comprises two branches, one branch is communicated with the convection section of the reforming reaction furnace, and the bottom oil heated from the convection section of the reforming reaction furnace is communicated with the prefractionating tower through a hot oil output pipe; and the other branch of the bottom oil output pipe is communicated with the inlet of the cold flow pipeline of the pre-hydrogenation feeding heat exchanger.
2. The reforming pretreatment system of claim 1, wherein the pre-hydrogenation feed heat exchanger sequentially connects the pre-hydrogenation heating furnace and the pre-hydrogenation reactor through a pipeline, and a reaction product outlet is arranged at the bottom of the pre-hydrogenation reactor and is communicated with a heat flow pipeline inlet of the pre-hydrogenation feed heat exchanger through a pipeline.
3. The reforming pretreatment system of claim 1, further comprising a stripper feed heat exchanger, a pre-hydrogenated product air cooler, a pre-hydrogenated product water cooler and a pre-hydrogenated liquid separation tank, wherein a hot flow inlet of the stripper feed heat exchanger is communicated with a hot flow outlet of the pre-distillation column feed heat exchanger, a hot flow outlet of the stripper feed heat exchanger is sequentially communicated with the pre-hydrogenated product air cooler, the pre-hydrogenated product water cooler and the pre-hydrogenated liquid separation tank through pipelines, a bottom oil outlet is arranged at the bottom of the pre-hydrogenated liquid separation tank, and the bottom oil outlet is communicated with a cold flow inlet of the stripper feed heat exchanger through a pipeline.
4. The reforming pretreatment system of claim 3, wherein the stripper column feed heat exchanger is further provided with a cold flow outlet, the cold flow outlet of the stripper column feed heat exchanger is communicated with the cold flow inlet of the stripper column bottom heat exchanger through a pipeline, and the cold flow outlet of the stripper column bottom heat exchanger is communicated with the stripper column through a pipeline.
5. The reforming pretreatment system of claim 4, wherein the bottom of the stripping tower is provided with a refined oil outlet, the refined oil outlet is communicated with the heat flow inlet of the bottom heat exchanger of the stripping tower, and the heat flow outlet of the bottom heat exchanger of the stripping tower is connected with the reforming reaction system.
6. The reforming pretreatment system of claim 5, wherein the pipeline connected with the refined oil outlet is provided with two branches, one branch is communicated with the stripper still heating furnace, the stripper still heating furnace is communicated with the stripper through a pipeline, and the other branch is communicated with the heat flow inlet of the stripper bottom heat exchanger.
7. A reforming processing system comprising the reforming pretreatment system according to any one of claims 1 to 6.
8. A method of reforming pretreatment of a reforming pretreatment system according to any one of claims 1 to 6, comprising: and (2) performing heat exchange and temperature rise on the bottom oil generated by the pre-fractionating tower by using a pre-hydrogenation feeding heat exchanger, then entering a pre-hydrogenation heating furnace for temperature rise, entering a pre-fractionating tower feeding heat exchanger for temperature rise after heat exchange and temperature reduction of a heat source in the pre-hydrogenation feeding heat exchanger, and introducing the heated feeding into the pre-fractionating tower.
9. The reforming pretreatment method according to claim 8, wherein the product after the reaction in the pre-hydrogenation reactor enters a hot flow inlet of a pre-hydrogenation feed heat exchanger, and the bottom oil generated by the pre-distillation tower is subjected to heat exchange and temperature rise in the pre-hydrogenation feed heat exchanger.
10. The method of claim 9, wherein the product of the pre-hydrogenation reactor after the pre-hydrogenation reaction is cooled by heat exchange in the pre-hydrogenation feed heat exchanger, and then introduced into the pre-fractionation column feed heat exchanger to heat the feed, and the cooled pre-hydrogenation reaction product is introduced into the stripping column feed heat exchanger.
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| CN103725313B (en) * | 2012-10-10 | 2017-07-07 | 中国石油化工集团公司 | The B-grade condensation separation method and device of catalytic reforming pre-hydrotreating reaction product |
| CN105647581B (en) * | 2014-11-12 | 2017-09-15 | 中国石油天然气股份有限公司 | Gasoline hydrogenation method |
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