CN112280589B - Catalytic-atmospheric-vacuum-hydrogenation heat combination device - Google Patents
Catalytic-atmospheric-vacuum-hydrogenation heat combination device Download PDFInfo
- Publication number
- CN112280589B CN112280589B CN202010918845.4A CN202010918845A CN112280589B CN 112280589 B CN112280589 B CN 112280589B CN 202010918845 A CN202010918845 A CN 202010918845A CN 112280589 B CN112280589 B CN 112280589B
- Authority
- CN
- China
- Prior art keywords
- oil
- heat
- hydrogenation
- heat exchanger
- slurry
- 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
- C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
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)
Abstract
The catalytic-atmospheric and vacuum-hydrogenation heat combined device is divided into a catalytic-atmospheric and vacuum device heat combined unit and an atmospheric and vacuum-hydrogenation device heat combined unit, a heat exchanger is adopted to replace a traditional heating furnace, and a low-temperature heat source is heated by high-temperature waste heat so as to achieve the aim of saving refinery fuel gas; the catalytic-atmospheric and vacuum device heat combination unit exchanges heat between slurry oil and crude oil through two slurry oil-crude oil heat exchangers, and heats the crude oil of the low-temperature atmospheric and vacuum device by using waste heat at a higher temperature of the catalytic device; the atmospheric and vacuum-hydrogenation unit replaces a reaction furnace and a reboiling furnace of the hydrogenation unit by the residual oil-hydrogenation raw oil heat exchanger and the residual oil-hydrogenation product heat exchanger, so that the hydrogenation unit does not consume fuel gas any more, and the purpose of saving fuel gas is achieved. The invention has ingenious conception, fully utilizes the waste heat of the device to replace fuel gas to heat low-temperature oil products, reasonably recycles the waste heat energy level, can greatly reduce the oil refining processing cost, and obtains better economic benefit.
Description
Technical Field
The invention belongs to the technical field of petroleum processing, and relates to a heat combined device, in particular to a catalytic-atmospheric-vacuum-hydrogenation heat combined device.
Background
The petroleum processing process is to carry out raw material reaction and product distillation at high temperature (370-800 ℃), and in order to realize high-temperature production, a refinery consumes a large amount of fuel gas and coke to provide high-temperature heat energy (hereinafter referred to as primary heat energy) for the petroleum refining production process. In the heating process of various oil products, most of the primary heat energy is transferred into products to become product enthalpy (hereinafter referred to as secondary heat energy), wherein the secondary heat energy is the most heavy oil processing devices such as catalysis, coking and the like. In order to reduce the energy consumption of the device, the secondary heat is generally exchanged with the raw oil of the device, so that the aims of reducing the fuel gas consumption of the device and increasing the economic benefit are fulfilled. However, the secondary heat of a part of the device is excessive, and a large amount of residual heat (hereinafter referred to as waste heat) is generated after the heat exchange with the raw oil, wherein the largest waste heat of the device is provided with about 5-7.6 tons of standard oil/hour of the catalytic device, about 3-6 tons of standard oil/hour of equivalent heavy oil processing device of the coking device, and the total amount of waste heat of a medium-large-scale refinery is estimated to be about 10-30 tons of standard oil/hour.
In order to save energy and increase efficiency, the waste heat must be recovered in the oil refining production process, and the current method is used for self-using a middle-pressure steam supply device and a low-pressure steam supply device, so that the purposes of reducing steam supply of a self-contained power station and saving boiler fire coal are achieved. In general, large and medium-sized refineries, particularly refineries for processing heavy crude oil, have a large amount of waste heat, and the amount of steam produced by waste heat can reach 200-300 tons/hour, which is estimated to be equivalent to 15-23 tons of standard oil/hour, about 13-20 ten thousand tons of standard oil/year equivalent heat energy, according to empirical data (13 tons of steam produced by catalytic residual boiler/ton of standard oil). The total amount of domestic refinery waste heat can be up to 800-1200 ten thousand tons of standard oil per year according to the data.
Further research finds that the oil refining system is energy-saving by using waste heat to produce steam, the energy consumption statistical value of the device is reduced, and the use of coal coke is reduced in a power station. However, it is an energy-saving technology with no economic benefit for refineries, and increases the petroleum processing cost of enterprises. The method has 200-300 refineries in China, the crude oil processing amount reaches more than 6 hundred million tons, and the waste heat utilization technology of a large number of devices has no economic benefit, so that the method is a huge economic loss for the whole industry, and also becomes a huge challenge in the energy saving technical field of China. Therefore, it is urgent to find a new way of waste heat utilization with good economic benefit and energy saving.
Aiming at the problems existing in the utilization of waste heat of a refinery, china patent No. CN201410100130.2 discloses a normal pressure reducing device for replacing fuel of a heating furnace with waste heat of catalytic flue gas and slurry oil, which mainly comprises the steps that the catalytic slurry oil and the second heat energy are sent to a heat exchanger for the normal pressure reducing device to exchange heat with crude oil. However, the precondition for realizing heat exchange is that a heat transfer temperature difference of 10-20 ℃ is needed between the high-temperature oil product and the low-temperature oil product. However, the final temperature of crude oil heat exchange before the application of the patent is about 280 ℃, the heat transfer temperature difference between 260-270 ℃ of the end temperature of the oil slurry heat exchange of the catalytic device is negative, and the heat transfer process cannot be realized. Therefore, in order to solve the problem of heat transfer temperature difference, the atmospheric and vacuum device is greatly transformed, so the defects of complex transformation, high difficulty and high investment exist. In addition, in the heat exchange process of the atmospheric and vacuum product and crude oil, the crude oil is heated from the initial temperature of 40 ℃ to the final temperature of 280 ℃ after the heat exchange of vacuum residue, wax oil, diesel oil and middle section reflux and crude oil. Wherein the last product exchanging heat with crude oil is residual oil, and the highest temperature (420 ℃) heat is the most. If the heat energy of the slag reduction high temperature level is about 2-3 tons of standard oil per hour and is 420-350 ℃, different crude oil heat exchange is carried out by the atmospheric and vacuum device, the final temperature of the crude oil heat exchange can be reduced to 240 ℃, and the heat combination of the atmospheric and vacuum-catalytic device is ensured to be smoothly implemented.
The refinery has several sets of product hydrogenizing units for gasoline, naphtha, chemical diesel oil, wax oil, etc. in the product hydrofining process, two heating furnaces, one reaction furnace and one fractionating tower bottom reboiling furnace, the temperature range gp of the oil heated by fuel gas is lower by 320-370 deg.c, and the total heat consumption of two furnaces in one unit is about 1.5-2 tons per hour. Therefore, the high-temperature (350-420 ℃) residual oil is combined with the oil products of the two heating furnaces in a heat mode, and the two heating furnaces are replaced by a heat exchanger to heat the two oil products, so that the heat energy of the residual oil sent out of the atmospheric and vacuum device is reasonably utilized.
Disclosure of Invention
The invention aims to solve the technical problem of providing the catalytic-atmospheric-vacuum-hydrogenation heat combined device which is reasonable in structural design and good in energy-saving effect.
The technical scheme adopted for solving the technical problems is as follows: a catalytic-atmospheric-vacuum-hydrogenation heat combination device, which is characterized in that: the heat-combined device consists of a catalysis-atmospheric and vacuum device heat-combined unit and an atmospheric and vacuum-hydrogenation device heat-combined unit,
the catalytic-atmospheric and vacuum device heat combination unit comprises a catalytic fractionating tower and two slurry-crude oil heat exchangers, wherein the two slurry-crude oil heat exchangers are sequentially arranged, the bottom of the catalytic fractionating tower is connected with a slurry pump through a first pipeline, the outlet of the slurry pump is connected with the first slurry-crude oil heat exchanger through a slurry pump outlet pipeline, the outlet end of the first slurry-crude oil heat exchanger is connected with the inlet end of a second slurry-crude oil heat exchanger, crude oil is sequentially connected with the second slurry-crude oil heat exchanger and the first slurry-crude oil heat exchanger through a second pipeline, and slurry flowing out of the bottom of the catalytic fractionating tower sequentially flows into the first slurry-crude oil heat exchanger and the second slurry-crude oil heat exchanger of the atmospheric and vacuum device after being subjected to heat exchange with crude oil through a third pipeline;
the heat combination unit of the atmospheric and vacuum-hydrogenation device comprises a vacuum tower, a residual oil-hydrogenation raw oil heat exchanger and a residual oil-hydrogenation product heat exchanger, wherein the bottom of the vacuum tower is connected with a residual oil pump through a fourth pipeline, the residual oil pump is divided into two paths after entering the hydrogenation device through a residual oil pump outlet pipeline, the first path is connected with a first residual oil-hydrogenation raw oil heat exchanger, and the other end of the first residual oil-hydrogenation raw oil heat exchanger is connected with the atmospheric and vacuum device through a pipeline; the second path is connected with a second residual oil-hydrogenation product heat exchanger, and the other end of the second residual oil-hydrogenation product heat exchanger is connected with the atmospheric and vacuum device through a pipeline; the raw oil is connected with a first residual oil-hydrogenation raw oil heat exchanger through a fifth pipeline, the bottom of the fractionating tower is connected with a second residual oil-hydrogenation product heat exchanger, oil residues from the vacuum tower respectively enter the first residual oil-hydrogenation raw oil heat exchanger, the second residual oil-hydrogenation product heat exchanger exchanges heat with residual oil and then returns to the atmospheric and vacuum device through a pipeline, and the raw oil enters the hydrogenation reactor after being subjected to heat exchange by the first residual oil-hydrogenation raw oil heat exchanger; and (3) exchanging heat of the oil product flowing out of the bottom of the fractionating tower through a second residual oil-hydrogenation product heat exchanger, and returning the oil product to the fractionating tower through a pipeline for continuous distillation.
As an improvement, the third pipeline is connected with the slurry oil-second middle heat exchanger, the slurry oil heat-exchanging effluent atmospheric and vacuum device returns to the catalytic device through the third pipeline, and enters the slurry oil-second middle heat exchanger to exchange heat with the recycle oil and then enters the vaporization section of the catalytic fractionating tower to flow downwards.
And the fifth pipeline is provided with a raw material pump and a third control valve, two raw material product heat exchangers are arranged between the raw material pump and the first residual oil-hydrogenation raw material oil heat exchanger, the bottom of the hydrogenation reactor is provided with a sixth pipeline which is connected with the two raw material product heat exchangers, and the raw material oil enters the first residual oil-hydrogenation raw material heat exchanger after heat exchange between the raw material product heat exchanger and a product discharged from the hydrogenation reactor.
Further, the hydrogenation device also comprises a water cooler, a high-pressure separator and a low-pressure separator which are sequentially connected, products from the hydrogenation reactor enter the water cooler after the heat exchange between the raw material product heat exchanger and the raw material oil, then enter the high-pressure separator and the low-pressure separator through pipelines to separate products from hydrogen, and then enter the fractionating tower through a seventh pipeline to distill and remove light oil products.
Further, a booster pump and a fourth control valve are arranged on an eighth pipeline between the fractionating tower and the second residue oil-hydrogenation product heat exchanger.
Further, a first control valve is arranged on the first pipeline, and a second control valve is arranged on the residual oil pump outlet pipeline.
And finally, the temperature of the slurry oil flowing out of the bottom of the catalytic fractionating tower is 350-360 ℃, the temperature of the slurry oil is reduced to 260 ℃ after the slurry oil exchanges heat with crude oil through a first slurry oil-crude oil heat exchanger and a second slurry oil-crude oil heat exchanger, and the temperature is increased to 300-320 ℃ after the crude oil exchanges heat.
Compared with the prior art, the invention has the advantages that: the device is divided into a catalytic-atmospheric and vacuum device heat combination unit and an atmospheric and vacuum-hydrogenation device heat combination unit, a heat exchanger is adopted to replace a traditional heating furnace, and a low-temperature heat source is heated by high-temperature waste heat, so that the purpose of saving fuel gas of a refinery is achieved; the catalytic-atmospheric and vacuum device heat combination unit exchanges heat between slurry oil and crude oil through two slurry oil-crude oil heat exchangers, and heats the crude oil of the low-temperature atmospheric and vacuum device by using waste heat at a higher temperature of the catalytic device; the atmospheric and vacuum-hydrogenation unit replaces a reaction furnace and a reboiling furnace of the hydrogenation unit by the residual oil-hydrogenation raw oil heat exchanger and the residual oil-hydrogenation product heat exchanger, so that the hydrogenation unit does not consume fuel gas any more, and the purpose of saving fuel gas is achieved. The invention has ingenious conception, fully utilizes the waste heat of the device to replace fuel gas to heat low-temperature oil products, reasonably recycles the waste heat energy level, can greatly reduce the oil refining processing cost, and obtains better economic benefit.
Drawings
FIG. 1 is a flow chart of a refinery atmospheric and vacuum, catalytic, and hydrogenation heat combination unit of example 1 provided by the invention;
FIG. 2 is a flow chart of a refinery hydrogenation unit according to example 1 provided by the present invention;
FIG. 3 is a flow chart of a comparative refinery hydrogenation unit provided by the present invention.
Detailed Description
The invention is described in further detail below with reference to the embodiments of the drawings.
Comparative example
As shown in fig. 3, hydrogenated raw oil (wax oil, diesel oil, aviation kerosene, naphtha gasoline, etc., hereinafter referred to as raw material) enters a raw material pump 4a through a pipeline 1a to be pressurized and then flows out of a pipeline 2a, new hydrogen is injected into the raw material through a pipeline 3a in the middle, circulating hydrogen is injected into the raw material through a pipeline 15a, and then the raw material flows into raw material-product heat exchangers 5 and 6 to exchange heat with a product discharged from a hydrogenation reactor 9. Then, the raw material is discharged from the raw material-product heat exchanger 6 and enters the raw material heating furnace 8a through the pipeline 7a to heat the raw material to 370 ℃ by using fuel gas, and then the raw material is discharged from the heating furnace 8a and enters the hydrogenation reactor 9 through the pipeline 35a to carry out impurity reactions such as desulfurization and nitrogen, and after the reaction is finished, the raw material is changed into a product and enters the product distillation system. Firstly, after the heat exchange temperature of the hydrogenation product flowing into the product-raw oil heat exchangers 6 and 5 and the raw oil is reduced through a pipeline 10a, the hydrogenation product flows into the water cooler 12 through a pipeline 11a for further cooling, and then enters the high-pressure separator 13 through a pipeline to separate out circulating hydrogen and returns to the raw oil pipeline 2a through a heat exchanger 15 a; the product after separating the recycle hydrogen flows into a low-pressure separator 16 through a pipeline 14a to separate the product from the hydrogen, and then the product is distilled to remove light oil products through a pipeline 17a to a fractionating tower 18. Because the temperature of the tower bottom product is lower, the product flows out from the tower bottom and enters the booster pump 50 through the pipeline 19a, then enters the reboiler 20a through the pipeline, the product with lower temperature at the tower bottom is heated to 370 ℃ by fuel gas, and then returns to the fractionating tower 18 through the pipeline 21a to continue to distill and produce the separated gas phase product.
Example 1
As shown in figure 1, the catalytic-atmospheric and vacuum-hydrogenation heat combination device consists of a catalytic-atmospheric and vacuum device heat combination unit and an atmospheric and vacuum-hydrogenation device heat combination unit.
The catalytic-atmospheric and vacuum unit heat combination unit comprises a catalytic fractionating tower 2 and two slurry-crude oil heat exchangers 24 and 25, wherein the two slurry-crude oil heat exchangers 24 and 25 are sequentially arranged, the bottom of the catalytic fractionating tower 2 is connected with a slurry pump 7 through a first pipeline 18, the outlet of the slurry pump 7 is connected with the first slurry-crude oil heat exchanger 24 through a slurry pump outlet pipeline 9, the outlet end of the first slurry-crude oil heat exchanger 24 is connected with the inlet end of a second slurry-crude oil heat exchanger 25, crude oil is sequentially connected with the second slurry-crude oil heat exchanger 25 and the first slurry-crude oil heat exchanger 24 through a second pipeline 27, slurry flowing out of the bottom of the catalytic fractionating tower 2 after being pressurized by the slurry pump 7 sequentially flows into the first slurry-crude oil heat exchanger 24 and the second slurry-crude oil heat exchanger 25 of the atmospheric and vacuum unit after being subjected to heat exchange with the crude oil, returns to the catalytic device through a pipeline 10 through a third pipeline, enters the slurry-middle heat exchanger 3 and flows downwards into the catalytic fractionating tower 2 after being subjected to the same cycle heat exchange. The temperature of the slurry oil flowing out of the bottom of the catalytic fractionating tower 2 is 350-360 ℃, the temperature of the slurry oil is reduced to about 260 ℃ after the slurry oil exchanges heat with crude oil through a first slurry oil-crude oil heat exchanger 24 and a second slurry oil-crude oil heat exchanger 25, the crude oil enters a second section of residual oil-crude oil heat exchanger 26 to exchange heat with residual oil through a second pipeline 27, then the crude oil comes out of the other end of the second section of residual oil-crude oil heat exchanger 26 and sequentially enters the second slurry oil-crude oil heat exchanger 25, the first slurry oil-crude oil heat exchanger 24 exchanges heat with the slurry oil, the temperature is increased to 300-320 ℃ after the heat exchange, and then the crude oil comes out of the other end of the first slurry oil-crude oil heat exchanger 24 and enters the atmospheric and vacuum other equipment 12 through a pipeline 10.
The combined atmospheric and vacuum hydrogenation unit comprises a vacuum tower 20, a residual oil-hydrogenation raw oil heat exchanger 30 and another residual oil-hydrogenation product heat exchanger 31, wherein the bottom of the vacuum tower 20 is connected with a residual oil pump 22 through a fourth pipeline 70, the residual oil pump 22 is divided into two paths after entering the hydrogenation device through a residual oil pump outlet pipeline 23, a first path 33 is connected with a first residual oil-hydrogenation raw oil heat exchanger 30, and the other end of the first residual oil-hydrogenation raw oil heat exchanger 30 is connected with a residual oil-crude oil heat exchanger 26 of the atmospheric and vacuum device through a pipeline 37. The second path 36 is connected with the other residual oil-hydrogenation product heat exchanger 31, the other end of the second residual oil-hydrogenation product oil heat exchanger 31 is connected with an atmospheric and vacuum device pipeline 37 through a pipeline 38, and oil residues from the vacuum tower 20 respectively enter the first residual oil-hydrogenation raw oil heat exchanger 30 and the other residual oil-hydrogenation product heat exchanger 31 for heat exchange and then are discharged from the hydrogenation device and returned to the atmospheric and vacuum device through the pipeline 37.
After heat exchange with products in the hydrogenation device, the hydrogenated raw oil is connected with a first residual oil-hydrogenated raw oil heat exchanger 30 through a fifth pipeline 34, the raw oil enters the hydrogenation reactor 9 after heat exchange of the first residual oil-hydrogenated raw oil heat exchanger 30, the bottom of the fractionating tower 18 is connected with a second residual oil-hydrogenated product heat exchanger 31, and the oil product flowing out of the bottom of the fractionating tower 18 is returned to the fractionating tower 18 for continuous distillation through the pipeline after heat exchange of the residual oil-hydrogenated product heat exchanger 31.
The specific flow of the hydrogenation unit is shown in fig. 2, the fifth pipeline 34 is connected with the raw oil pipeline 1, a raw oil pump 4 and a third control valve 41 are arranged on the raw oil pipeline 1, two raw oil product heat exchangers 5 and 6 are arranged between the raw oil pump 4 and the first residual oil-hydrogenation raw oil heat exchanger 30, a sixth pipeline 91 is arranged at the bottom of the hydrogenation reactor 9 and is connected with the two raw oil product heat exchangers 6 and 5, and raw oil enters the first residual oil-hydrogenation raw oil heat exchanger 30 after heat exchange between the raw oil product heat exchangers 5 and 6 and the product discharged from the hydrogenation reactor 9.
The hydrogenation device also comprises a water cooler 12, a high-pressure separator 13 and a low-pressure separator 16 which are sequentially connected, wherein products from the hydrogenation reactor 9 enter the water cooler 12 after heat exchange between raw material product heat exchangers 6 and 5 and raw material oil, then enter the high-pressure separator 13 through a pipeline to separate out circulating hydrogen, return the circulating hydrogen to the raw material oil pipeline 1 through a pipeline 15, flow into the low-pressure separator 16 through the pipeline to separate products from hydrogen, and then enter a fractionating tower 18 through a seventh pipeline 17 to distill and remove light oil products. A booster pump 50 and a fourth control valve 29 are arranged on the eighth pipeline 19 between the fractionating tower 18 and the second residuum-hydrogenation product heat exchanger 31.
The residual oil of the atmospheric and vacuum device which is thermally combined with the hydrogenation device enters the hydrogenation device through the pipeline B and is divided into two paths, wherein the first path enters the hydrogenation raw material-residual oil heat exchanger 30 through the pipeline 23 to replace a heating furnace 8a for heating raw material oil, then the residual oil flows out of the heat exchanger 30 to enter a pipeline 37, the other path enters the product-residual oil heat exchanger 31 through the pipeline 36 to replace the heating furnace 20a for heating product oil, and then the residual oil flows out of the heat exchanger 31 through the pipeline 37 to be returned to the atmospheric and vacuum device through the pipeline 37 to the a-outlet device.
The specific process flow is as follows:
the waste heat of the catalytic device is about 4-5 tons of standard oil/hour, the temperature is about 340-350 ℃, the slurry oil is used as a heat carrier, and the crude oil with the temperature of about 240 ℃ is sent to the atmospheric and vacuum device to be heated, so that the final heating temperature of the crude oil reaches 300-320 ℃. The slurry oil flows out from the bottom of the catalytic fractionating tower 2, enters the slurry oil pump 7 through the first pipeline 18 to be pressurized, flows into the slurry oil-crude oil heat exchanger 24 and 25 of the atmospheric and vacuum device through the pipeline 9 to exchange heat with crude oil, then returns to the catalytic device through the pipeline 10, enters the slurry oil-second heat exchanger 3 to exchange heat with oil with the temperature of 330-350 ℃ to rise to about 270-280 ℃, enters the slurry oil-second heat exchanger 3 to enter the vaporization section of the catalytic fractionating tower 2 to flow downwards, then flows into the tower bottom through the first pipeline 18 to flow into the slurry oil pump 7 after contacting with the high-temperature 430 ℃ reaction oil gas flowing into the tower through the pipeline 80 to rise to the temperature of 350-360 ℃, and is repeatedly circulated in this way to feed the catalytic waste heat into the crude oil.
The atmospheric and vacuum-hydrogenation heat combination is that the residue at the bottom of the atmospheric and vacuum device is sent to a hydrogenation device. The first-stage heat exchange of residual oil and crude oil is canceled, the residual oil at the bottom of the vacuum tower 20 is directly fed into a hydrogenation device, one residual oil-hydrogenation raw oil heat exchanger 30 is used for replacing the raw oil furnace 8a to heat the raw oil, and the other residual oil-hydrogenation product heat exchanger 31 is used for replacing the reboiler furnace 20a to heat the product, so that the purposes of canceling the heating of the two heating furnaces and saving fuel gas are achieved. Then, the residual oil with the temperature reduced to about 300-360 ℃ returns to the atmospheric and vacuum device and enters a second-section residual oil-crude oil heat exchanger according to the original flow;
residue at 420 ℃ at the bottom of the atmospheric and vacuum device vacuum tower 20 flows into a residue pump 22 through a pipeline 70 for pressurization, flows out of the atmospheric and vacuum device through a residue pump outlet pipeline 23 to enter a hydrogenation device, and then is divided into two paths: the first path flows into the residual oil-hydrogenation raw oil heat exchanger 30 through a pipeline 33 to be exchanged with raw oil so as to cancel the raw material heating furnace 8a, and then the residual oil is discharged out of the first residual oil-hydrogenation raw oil heat exchanger 30 and returned to the atmospheric and vacuum device through a pipeline 37. The second pipeline flows into the second residue-hydrogenation product heat exchanger 31 through a pipeline 36 to exchange heat with the bottom oil of the product distillation tower to achieve the purpose of eliminating the bottom reboiling furnace 20a, then the residue flows out of the second residue-hydrogenation product heat exchanger 31 through a pipeline 38 into a pipeline 37 to return to the atmospheric and vacuum device, enters the residue-crude oil heat exchanger 26, then exits the residue-crude oil heat exchanger 26 to the coking device through a pipeline 28.
The hydrogenated raw oil enters the raw pump 4 through the raw oil pipeline 1 and flows out of the raw oil pipeline 34 after being pressurized, new hydrogen is injected into the raw oil through the pipeline 90, and the circulating hydrogen is injected into the raw oil through the pipeline 15 and then flows into the raw material-product heat exchangers 5 and 6 through the raw oil pipeline to exchange heat with the product discharged from the hydrogenation reactor. And then the discharged raw material-product heat exchanger 6 enters the first residual oil-hydrogenation raw material heat exchanger 30 through a fifth pipeline 34 to exchange heat with the vacuum residual oil at 420 ℃ and then the temperature is increased to 310-340 ℃. The raw oil enters a hydrogenation reactor 9 through a pipeline 35 to carry out impurity reactions such as desulfurization nitrogen and the like, after the reaction is finished, the hydrogenation product flows into a raw product heat exchanger 6 and 5 through a pipeline 91 to exchange heat with the raw oil to reduce the temperature to about 250 ℃, then flows into a water cooler 12 through the pipeline to be further cooled, and then enters a high-pressure separator 13 to separate out recycle hydrogen and returns to the raw oil pipeline through a pipeline 15; the product after separating the recycle hydrogen flows into a low-pressure separator 16 to separate the product from the hydrogen, and then the product is distilled by a fractionating tower 18 through a seventh pipeline 17 to remove light oil. Because the temperature of the tower bottom product is lower, the product flows out of the tower bottom, enters the booster pump 50 through the pipeline 19, enters the second residue oil-hydrogenation product heat exchanger 31 through the pipeline to exchange heat with the residue oil at 420 ℃, then the temperature of the hydrogenation product is raised to 330-350 ℃, and then returns to the fractionating tower 18 through the pipeline to continue to distill to produce the separated gas phase product.
The following describes the improved idea of the present invention:
the invention utilizes the waste heat of the high temperature position of the device to heat the low temperature heat source, thereby achieving the purpose of saving the fuel gas of the refinery. The high temperature waste heat selected by the invention has two units, one is the slurry oil of the catalytic device and the waste heat in the second (called catalytic waste heat below), the temperature is about 350-360 ℃, and the other is the waste heat of the vacuum residue of the atmospheric and vacuum device, and the temperature is 420 ℃. The low-temperature oil product heat source (hereinafter referred to as low-temperature heat source) needing heating is provided with two units as well, one unit is a hydrogenation device, and comprises three products of naphtha and gasoline hydrogenation, diesel and aviation kerosene hydrogenation, wax hydrogenation and the like, the hydrofining device is provided with a reaction furnace and a reboiling furnace at the bottom of a fractionating tower, the temperature range of the oil product heated by fuel gas is about 310-350 ℃ lower, and the total heat consumption of two furnaces in one device is about 1.5-2 tons per hour; the other unit is the atmospheric and vacuum packed crude oil, the heating temperature is about 300-320 ℃, and the heat consumption is about 3-4 tons of standard oil/hour.
The two device heat energy combined units are formed by the method of optimizing pairing according to the thought: one is a catalytic-atmospheric and vacuum device heat combination unit, which uses the waste heat of the higher temperature position of the catalytic device to heat the crude oil of the low temperature position atmospheric and vacuum device; the other is an atmospheric and vacuum-hydrogenation unit heat combination unit, namely, the atmospheric and vacuum device vacuum residue is used for replacing a reaction furnace of the hydrogenation unit and a reboiling furnace to heat low-temperature oil products entering the two furnaces, so that the purpose of saving fuel gas of the atmospheric and vacuum device and the hydrogenation device is achieved. The equivalent heat value cost of the refinery fuel gas is similar to the cost of the industrial natural fuel gas by about 3000-4000 yuan/ton standard oil and is 4-5 times of the cost of the coal coke, so that the waste heat of the device is used for replacing fuel gas to heat low-temperature oil products, and the processing cost of the refinery fuel gas can be greatly reduced.
The economic benefits produced after implementation are analyzed as follows:
1. saving fuel gas
Taking 300 ten thousand tons/year catalytic converter 1000 ten thousand tons/year atmospheric and vacuum converter and 200 ten thousand tons/year diesel hydrogenation unit as examples, the catalytic slurry waste heat is about 4.4 tons of standard oil/hour for heating crude oil of the atmospheric and vacuum converter, so that the atmospheric and vacuum reduction reduces fuel gas consumption by 4.4 tons of standard oil/hour. Before the patent implementation of the heat exchanger, heat energy in the temperature range of 420-160 ℃ of residual oil of the atmospheric and vacuum device exchanges heat with crude oil, so that the fuel gas consumption of the same heat quantity is reduced. After the patent implements the combination of atmospheric and vacuum pressure and hydrogenation heat, the heat energy of the residual oil at 420-350 ℃ is removed from the hydrogenation device to realize heat combination, about 1.5-2 tons of standard oil/hour gas is saved by canceling two heating furnaces for hydrogenation, the temperature of the residual oil is reduced to about 350 ℃ when the residual oil returns to atmospheric and vacuum pressure, and therefore, the heat energy of the residual oil and crude oil heat exchange capacity is reduced by about 1.5-2 tons of standard oil heat energy and the hydrogenation gas saving amount are the same, and the heat energy and the hydrogenation gas saving amount are mutually offset. Thus, by combining the results, a certain refinery actually saves the fuel gas by 4.4 tons of standard oil per hour, the fuel gas price is about 4000 yuan/ton, and the fuel gas production value is 1.76 ten thousand yuan/hour, 1.53 hundred million yuan/year.
2. Simple flow and low equipment investment
The patent implementation is compared with the equipment before and after, 4 heating furnaces are reduced, 4 heat exchangers are added, 1 oil pump is arranged, and 2000 meters of pipelines are arranged.
3. Social benefits
By implementing the patent, a ten million-ton refinery can save 3.83 ten thousand tons of standard oil natural gas each year. There are 100 large-scale refineries in the whole country, and the conservation estimation can reduce 300 ten thousand tons of standard oil of refinery gas each year. The functions of the refinery fuel gas are completely the same as those of the natural gas, and many refineries need to outsource the natural gas because the fuel gas produced by the refineries is insufficient. Therefore, the refinery can save fuel gas by adopting the patent and can relieve the contradiction between domestic natural gas supply and demand.
Claims (4)
1. A catalytic-atmospheric-vacuum-hydrogenation heat combination device, which is characterized in that: the heat-combined device consists of a catalysis-atmospheric and vacuum device heat-combined unit and an atmospheric and vacuum-hydrogenation device heat-combined unit,
the catalytic-atmospheric and vacuum device heat combination unit comprises a catalytic fractionating tower and two slurry-crude oil heat exchangers, wherein the two slurry-crude oil heat exchangers are sequentially arranged, the bottom of the catalytic fractionating tower is connected with a slurry pump through a first pipeline, the outlet of the slurry pump is connected with the first slurry-crude oil heat exchanger through a slurry pump outlet pipeline, the outlet end of the first slurry-crude oil heat exchanger is connected with the inlet end of a second slurry-crude oil heat exchanger, crude oil is sequentially connected with the second slurry-crude oil heat exchanger and the first slurry-crude oil heat exchanger through a second pipeline, and slurry flowing out of the bottom of the catalytic fractionating tower sequentially flows into the first slurry-crude oil heat exchanger and the second slurry-crude oil heat exchanger of the atmospheric and vacuum device after being subjected to heat exchange with crude oil through a third pipeline;
the heat combination unit of the atmospheric and vacuum device comprises a vacuum tower of the atmospheric and vacuum device, a residual oil-hydrogenation raw oil heat exchanger and a residual oil-hydrogenation product heat exchanger, wherein the bottom of the vacuum tower is connected with a residual oil pump through a fourth pipeline, the residual oil pump is divided into two paths after entering the hydrogenation device through a residual oil pump outlet pipeline, the first path is connected with the residual oil-hydrogenation raw oil heat exchanger, and the other end of the residual oil-hydrogenation raw oil heat exchanger is connected with the atmospheric and vacuum device through a pipeline; the second path is connected with a residual oil-hydrogenation product heat exchanger, and the other end of the residual oil-hydrogenation product heat exchanger is connected with the atmospheric and vacuum device through a pipeline; the hydrogenation unit raw oil is connected with a first residual oil-hydrogenation raw oil heat exchanger through a fifth pipeline, the bottom product of the fractionating tower is connected with a second residual oil-hydrogenation product heat exchanger through a pipeline, oil residues from the vacuum tower respectively enter the first residual oil-hydrogenation raw oil heat exchanger, the second residual oil-hydrogenation product heat exchanger exchanges heat with the raw oil and the product, and then the raw oil enters the hydrogenation reactor after exchanging heat with the first residual oil-hydrogenation raw oil heat exchanger; and (3) after the heat exchange of the product flowing out of the bottom of the fractionating tower by the second residue oil-hydrogenation product heat exchanger, returning the product to the fractionating tower through a pipeline for continuous distillation.
2. The catalytic-atmospheric-vacuum-hydrogenation heat combination unit according to claim 1, wherein: the third pipeline is connected with the oil slurry-second middle heat exchanger, and the oil slurry enters the oil slurry-second middle heat exchanger to exchange heat with the recycle oil and then enters the vaporization section of the catalytic fractionating tower to flow downwards.
3. The catalytic-atmospheric-vacuum-hydrogenation heat combination unit according to claim 1, wherein: the fifth pipeline is provided with a raw material pump, two raw material product heat exchangers are arranged between the raw material pump and the first residual oil-hydrogenation raw material oil heat exchanger, the bottom of the hydrogenation reactor is provided with a sixth pipeline which is connected with the two raw material product heat exchangers, and the raw material oil enters the first residual oil-hydrogenation raw material heat exchanger after heat exchange between the raw material-product heat exchanger and a product discharged from the hydrogenation reactor.
4. A catalytic-atmospheric-vacuum-hydrogenation heat combination unit according to any one of claims 1 to 3, characterized in that: the temperature of the slurry oil flowing out from the bottom of the catalytic fractionating tower is 350-360 ℃, the temperature of the slurry oil is reduced to 250-260 ℃ after the slurry oil exchanges heat with crude oil through a first slurry oil-crude oil heat exchanger and a second slurry oil-crude oil heat exchanger, and the temperature is increased to 300-320 ℃ after the crude oil exchanges heat.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010918845.4A CN112280589B (en) | 2020-09-04 | 2020-09-04 | Catalytic-atmospheric-vacuum-hydrogenation heat combination device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010918845.4A CN112280589B (en) | 2020-09-04 | 2020-09-04 | Catalytic-atmospheric-vacuum-hydrogenation heat combination device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112280589A CN112280589A (en) | 2021-01-29 |
| CN112280589B true CN112280589B (en) | 2023-08-04 |
Family
ID=74419740
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010918845.4A Active CN112280589B (en) | 2020-09-04 | 2020-09-04 | Catalytic-atmospheric-vacuum-hydrogenation heat combination device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112280589B (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201737903U (en) * | 2010-05-27 | 2011-02-09 | 上海九元石油化工有限公司 | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device |
| CN104927905A (en) * | 2014-03-18 | 2015-09-23 | 雷泽永 | Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device |
-
2020
- 2020-09-04 CN CN202010918845.4A patent/CN112280589B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201737903U (en) * | 2010-05-27 | 2011-02-09 | 上海九元石油化工有限公司 | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device |
| CN104927905A (en) * | 2014-03-18 | 2015-09-23 | 雷泽永 | Atmospheric and vacuum catalytic flue gas-oil slurry heat combined device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112280589A (en) | 2021-01-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3341590B1 (en) | Power generation from waste heat in integrated hydrocracking and diesel hydrotreating facilities | |
| EP3543487B1 (en) | Power generation from waste heat in integrated crude oil diesel hydrotreating and aromatics facilities | |
| EP3341575B1 (en) | Power generation using independent dual organic rankine cycles from waste heat systems in diesel hydrotreating-hydrocracking and continuous-catalytic-cracking-aromatics facilities | |
| US10961873B2 (en) | Power generation from waste energy in industrial facilities | |
| EP3341582B1 (en) | Power generation from waste heat in integrated aromatics, crude distillation, and naphtha block facilities | |
| EP3543486B1 (en) | Power generation from waste heat in integrated crude oil hydrocracking and aromatics facilities | |
| CN201737903U (en) | Heat integration system of distilling device, reforming device and gasoline and diesel hydrofining device | |
| CN112280589B (en) | Catalytic-atmospheric-vacuum-hydrogenation heat combination device | |
| CN113267075A (en) | Heat exchange system and heat exchange process for hydrogenation process | |
| CN217230628U (en) | Lubricating oil base oil production device | |
| CN212051181U (en) | System for utilizing waste heat in benzene hydrogenation technological process | |
| CN215288657U (en) | Gasoline hydrogenation system | |
| CN110511784A (en) | It is hydrocracked fractionating column tail oil heat utilization system and method | |
| CN105316039A (en) | Hydrogenation technology | |
| CN113801692A (en) | System and method for producing ethylene device raw material from residual oil |
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 |