CN108559545B - Residual oil hydrofining process for stopping and starting fractionating tower system and changing cold low fraction oil going direction - Google Patents
Residual oil hydrofining process for stopping and starting fractionating tower system and changing cold low fraction oil going direction Download PDFInfo
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- CN108559545B CN108559545B CN201810309441.8A CN201810309441A CN108559545B CN 108559545 B CN108559545 B CN 108559545B CN 201810309441 A CN201810309441 A CN 201810309441A CN 108559545 B CN108559545 B CN 108559545B
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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
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Abstract
The invention belongs to the technical field of petrochemical industry, and discloses a stop-start fractionating tower system and a residual oil hydrofining process for changing the cold low fraction oil heading direction. Self-cooling outletThe cold low-fraction oil of the low-fraction tank does not enter H any more after heat exchange2S stripper, but cooled and then reacted with H2Mixing unstable naphthas at the top of the S stripping tower, feeding the mixed naphthas to a gasoline and diesel oil hydrofining device for separation, and simultaneously stopping H2Fractionating column system after S-stripper and using H2And the bottom oil of the S stripping tower directly enters the primary raw material heat exchanger to heat the raw materials. The check shows that the invention has little investment and strong practicability, not only simplifies the operation, but also reduces the energy consumption by about 60 percent, and does not have any influence on the quality and the yield of the residual oil hydrogenation process and the refined residual oil. Is suitable for the reconstruction of old devices and the construction of new devices.
Description
Technical Field
The invention belongs to the technical field of petrochemical industry, and particularly relates to a residual oil hydrofining process for stopping and starting a fractionating tower system and changing the direction of cold low-fraction oil.
Background
The residual oil hydrorefining is a process for pretreating residual oil and providing raw materials for subsequent processing such as catalytic cracking. It consists of three parts of reaction, circulating hydrogen separation and product separation. In the reaction part, raw materials are subjected to heat exchange, mixed with circulating hydrogen and new hydrogen, sent to a reaction feeding heating furnace, heated to a specified temperature, sent to a reactor, subjected to reactions such as desulfurization, denitrification, demetalization and the like in a high-temperature, high-pressure and hydrogen-contacting environment, and accompanied with the generation of a small amount of naphtha and diesel oil. Thereafter, the reaction product leaves the reactor, exchanges heat with the feedstock, and then passes to the recycle hydrogen separation section.
The circulating hydrogen separation part consists of four units, namely a hot high-separation unit, a hot low-separation unit, a cold high-separation unit and a cold low-separation unit. Wherein, the cold high-molecular gas rich in hydrogen is sent to a recycle hydrogen compressor after being desulfurized and is returned to the reaction part for recycling after being pressurized; the cold low-pressure separation unit obtains cold low-pressure separation gas and cold low-pressure separation oil, the cold low-pressure separation gas is desulfurized and then is subjected to a hydrogen gas recovery system, and the cold low-pressure separation oil and hot low-pressure separation oil are subjected to heat exchange and temperature rise and then are sent to a product separation part.
The product separation part comprises three towers and one furnace, wherein the three towers are respectively H2S stripping tower, fractionating tower and side firewoodOil stripper and fractionating tower feed heating furnaces (the latter two towers and one furnace are simply called "fractionating system"). Wherein the cold and hot low-fraction oil from the recycle hydrogen separation part is firstly stripped in a stripping tower, and H in the stripping tower is dissolved under the action of medium-pressure steam2The gas phase impurities such as S and the like are removed from the tower top, unstable naphtha is sent to a gasoline and diesel oil hydrofining device, the liquid phase at the tower bottom is automatically pressed into a fractionating tower feeding heating furnace, heated to a specified temperature and then sent to the fractionating tower, through separation, the naphtha is obtained at the tower top, diesel oil is obtained at the lateral line, and the bottom oil, namely refined residual oil, is sent to a catalytic cracking device to be used as a raw material after being subjected to heat exchange with the raw material and the like and temperature reduction.
Obviously, in the residue hydrorefining process, which mainly aims at the pretreatment of the feedstock, the naphtha and diesel fractions resulting from cracking are few, generally not higher than 5%, due to the shallow depth of reaction, and are also mainly concentrated in the cold low-cut oil and constitute the main body of the cold low-cut oil. The existing residual oil hydrofining device does not perform flow combination with other devices with similar principles under the condition of low light oil yield, and is still provided with a complete product separation system, so that the defects of overlong separation flow and high energy consumption are caused.
Disclosure of Invention
In view of the defects and shortcomings of the prior art, the invention aims to provide a residual oil hydrofining process for stopping and starting a fractionating tower system and changing the cold low fraction oil to the cold low fraction oil. The process of the invention directly feeds the cold low-fraction oil into the gasoline and diesel hydrorefining device, and the cold low-fraction oil does not enter the downstream product separation part, so that the separation process aiming at obtaining naphtha and diesel oil after the stripping tower can be stopped. Greatly simplifies the flow and operation of the residual oil hydrofining device, reduces the energy consumption thereof, and simultaneously does not have any influence on the quality and yield of the refined residual oil.
The purpose of the invention is realized by the following technical scheme:
a residual oil hydrofining process for stopping and starting a fractionating tower system and changing the cold low fraction oil going direction comprises the following steps:
(1) the cold low-temperature oil discharged from the cold low-temperature oil separating tank does not enter H any more after being subjected to heat exchange with the hot low-temperature gas separating through the cold low-temperature oil separating primary-hot low-temperature gas separating primary heat exchanger2S stripper, andis cooled by circulating water through a cooler and then is mixed with H2Mixing unstable naphthas at the top of the stripping tower, and feeding the mixed naphthas to a gasoline and diesel oil hydrofining device for separation;
(2) shutdown H2The fractionating tower system after the S stripping tower comprises a fractionating tower feeding heating furnace, a fractionating tower, a side line diesel stripping tower bottom reboiler, a fractionating tower bottom oil pump, a fractionating tower top oil-gas-hot water heat exchanger, a fractionating tower top oil-gas secondary air cooling, a fractionating tower top oil-gas separation tank, a fractionating tower top cold reflux and a naphtha pump, wherein a raw material primary heat exchanger is reserved, and H is newly added2Pipeline from the bottom oil of S stripping tower to the primary heat exchanger of raw material to make H2And the bottom oil of the S stripping tower directly enters the primary raw material heat exchanger to heat the raw materials.
Further, the cooling by the circulating water in the step (1) means cooling to about 40 ℃.
Further, said H in step (2)2And a stripping tower bottom oil pump is arranged on a pipeline from the bottom oil of the S stripping tower to the primary raw material heat exchanger, and the stripping tower bottom oil pump is a fractionating tower bottom oil pump of the original shutdown fractionating tower system.
The invention is based on the following principle:
(1) the cold low-fraction oil is a low-temperature (about 50 ℃) condensate mixture of hot high-fraction gas and hot low-fraction gas, the main fractions are naphtha and diesel oil, almost no wax oil is contained, the properties of the cold low-fraction oil are very similar to those of the low-fraction oil of a diesel oil hydro-upgrading device or a gasoline and diesel oil hydro-refining device, and the cold low-fraction oil can be sent to the hydrogenation devices due to small flow, and the separation is completed by the aid of a fractionation system of the hydrogenation devices.
(2) The light fraction produced in the residual oil hydrogenation process is mainly concentrated in cold low-molecular oil, and the content in hot low-molecular oil is less, so that after the cold low-molecular oil is delivered out, H2The naphtha and diesel separation flow after the S stripping tower is not necessary to be reserved. While even the hot low-molecular oil contains a small amount of light fraction, the light fraction passes through the existing H2The unstable naphtha stream at the top of the S stripping tower can also be basically recovered.
(3) Due to H2The temperature and the flow of the bottom oil of the S stripping tower are slightly higher than those of the bottom oil of the fractionating tower for two times (the first time is usually used as a reboiling heat source of the diesel stripping tower), and the S stripping tower has equivalent propertiesTherefore, the method is completely feasible for heating the raw materials, and slightly increases the temperature of the raw materials after replacement, thereby helping to reduce the energy consumption of the reaction feeding heating furnace.
(4) The change proposed by the invention is concentrated in the circulating hydrogen separation and product separation part at the downstream of the device, and the temperature after the raw material is changed can be ensured, so that the upstream reaction part can not be influenced, and the quality and yield of the refined residual oil can not be changed.
Compared with the prior art, the invention has the following advantages and beneficial effects:
(1) the product fraction only retains H2And the flow and the operation of the S stripping tower are greatly simplified.
(2) Because the fractionating tower feeding heating furnace, the fractionating tower, the diesel oil stripping tower and the accessory equipment are shut down, the energy consumption of the device is reduced by about 60 percent.
(3) After the cold low oil is delivered, H2The feeding amount of the S stripping tower is reduced, the feeding temperature is increased, and the middle-pressure stripping steam consumption and the tower top cooling load are favorably reduced.
(4) The feeding temperature of the raw materials in the reaction feeding heating furnace is improved, which is beneficial to reducing the fuel consumption of the reaction feeding heating furnace.
(5) The change is concentrated at the downstream of the device, the core reaction part at the upstream is not influenced, and the quality and the yield of the refined residual oil are not changed.
(6) The invention is simple, the investment is little, only one H needs to be added2The pipeline from the bottom oil of the S stripping tower to the raw material heat exchanger, a pipeline from cold low-oil separation to unstable naphtha or a cold low-oil separation secondary circulating water cooler (which can utilize old equipment).
Drawings
FIG. 1 is a process flow diagram (feedstock throughput 228t/h) of a conventional residue hydrofinishing scheme in a comparative example of the present invention.
FIG. 2 is a process flow diagram (feedstock processing 228t/h) of a residue hydrofinishing scheme in an example of the present invention.
The numbering in the figures is as follows: 1-hot low-pressure separation tank; 2-a primary heat exchanger for cooling low-temperature oil to heating low-temperature gas; 3. secondary air cooling of hot low-pressure gas; 4-cooling and low-temperature separating tank; 5-cold secondary-diesel primary oil separation heat exchanger; 6. a pressure reducing valve; 7-a stripping tower; 8-oil gas air cooling at the top of the stripping tower; 9-a stripping tower top oil-gas separation tank; 10-stripping tower top cold reflux and naphtha pump; 11-fractionating tower feed heating furnace; 12-a fractionation column; 13-side stripper for diesel; 14-side diesel stripper bottoms reboiler; 15-fractionating tower bottom oil-raw material primary heat exchanger; 16-fractionation column bottoms pump; 17-fractionating tower top oil gas-hot water heat exchanger; 18-secondary air cooling of oil gas at the top of the fractionating tower; 19-fractionating tower top oil-gas separation tank; 20-fractionating tower top cold reflux and naphtha pump; 21-stripper bottoms oil pump; 22-cold low oil separation secondary circulating water cooler.
Detailed Description
The present invention will be described in further detail with reference to examples and drawings, but the present invention is not limited thereto.
Comparative example
The comparative example is the prior residual oil hydrofining process, and the process flow diagram is shown in figure 1. The specific process flow is as follows:
(1) the cold low-fraction oil (10.4t/H, 50 ℃ and 1.5Mpag) discharged from the cold low-fraction tank 4 passes through the cold low-fraction oil primary-hot low-fraction gas primary heat exchanger 2 and the cold low-fraction oil secondary-diesel primary heat exchanger 5 in sequence, exchanges heat with hot low-fraction gas and diesel to raise the temperature to 214.7 ℃, is mixed with the hot low-fraction oil (217.8t/H, 319.3 ℃ and 1.52Mpag) discharged from the hot low-fraction tank 1, is properly depressurized by a pressure reducing valve 6, and then is subjected to H reduction2And in the S stripping tower 7, hot low-pressure gas in the hot low-pressure tank 1 sequentially passes through the primary cold low-pressure oil-gas-hot low-pressure gas heat exchanger 2 and the secondary hot low-pressure gas air cooling 3 and then enters the cold low-pressure tank 4.
(2)H2The top pressure of the S stripping tower is 1.02Mpag, and the temperature is 146.8 ℃. The oil gas is cooled to 40 ℃ by air cooling 8 and then enters a separation tank 9. Separating out H-rich substances by three-phase separation234.2kg/h of S gas, 14.1t/h and 2.03t/h of cold reflux and unstable naphtha respectively, and about 3t/h of sewage. Corresponding to the cooling load 2396kw of air cooling 8. The cold reflux and the unstable naphtha are respectively returned to the tower and the gasoline and diesel oil feeding hydrofining device after being pressurized by the pump 10. At the same time, H2The S stripping tower consumes 3.5Mpag of stripping steam for 3.01t/h, and the temperature of the bottom of the S stripping tower is 311 ℃. The tower bottom oil is firstly self-pressurized into a fractionating tower feeding heating furnace 11, and the temperature is raisedAnd feeding the obtained product to a fractionating tower 12 at the temperature of 330.8 ℃, wherein the obtained product corresponds to 3504kw of effective heat load of a heating furnace (equivalent to about 354kg/h of standard fuel oil consumption).
(3) The pressure of the fractionating tower top is 0.069Mpag, and the temperature is 103.8 ℃. The oil gas at the tower top is cooled to 40 ℃ through a hot water heat exchanger 17 and an air cooling 18 in sequence and then enters a separation tank 19. Three-phase separation is carried out to obtain cold reflux of 16.2t/h and stable naphtha of 0.55t/h, and the cold reflux and the stable naphtha are respectively returned to the tower and taken out of the device after being pressurized by a pump 20. Corresponding to a total cooling load at the top of the column of 7021 kw. The diesel oil distilled from the side line of the fractionating tower enters a stripping tower 13, lighter naphtha fraction is gasified under the action of the heat of a reboiler 14, and the naphtha fraction returns to the fractionating tower through an overhead volatilization line, and the product diesel oil (11.7t/h) is obtained from the bottom. The product diesel oil is discharged out of the device after being cooled by a cold low oil separation secondary-diesel oil primary heat exchanger 5.
(4) The fractionating column consumed 1.0Mpag of stripping steam 7.06 t/h. The bottom oil (214.6t/h and 324 ℃) of the tower is used as a heat source of a side line diesel stripper reboiler 14 after passing through a fractionating tower bottom oil pump 16, after 1324kw of heat is released, the raw material is heated to 272 ℃ through a fractionating tower bottom oil-raw material primary heat exchanger 15, and the raw material is cooled by the heat exchanger and then is used as the raw material in a catalytic cracking device.
Examples
The process flow diagram of the residue hydrofining process of the embodiment is shown in fig. 2. Compared with the flow of the comparative example, the following improvements are implemented:
(1) the cold low-temperature oil discharged from the cold low-temperature oil separating tank 4 does not enter H any more after exchanging heat with the hot low-temperature gas after passing through the cold low-temperature oil separating primary-hot low-temperature gas separating primary heat exchanger 22The S stripping tower 7 is cooled to about 40 ℃ by circulating water through a cold low oil separation secondary circulating water cooler 22 and then is mixed with H2Mixing unstable naphthas at the top of the S stripping tower, and feeding the mixed naphthas to a gasoline and diesel oil hydrofining device (such as H of the S stripping tower)2S stripper) with the aid of which the separation of the gas, naphtha and diesel fractions is accomplished.
(2) Shutdown H2The process of the fractionating tower system after the S stripping tower 7 comprises a fractionating tower feeding heating furnace 11, a fractionating tower 12, a side line diesel stripping tower 13, a side line diesel stripping tower bottom reboiler 14, a fractionating tower bottom oil pump 16, a fractionating tower top oil gas-hot water heat exchanger 17, and a fractionating tower top oil gas secondary airCold 18, a fractionation overhead oil-gas separation tank 19, a fractionation overhead cold reflux and a naphtha pump 20. But the primary heat exchanger 15 of the raw material is reserved, and only the hot material flow is changed into H from the bottom oil of the fractionating tower2And (4) bottom oil of an S stripping tower.
(3) Adding a pipeline from the bottom oil of the stripping tower to the primary raw material heat exchanger 15 to heat the raw material by replacing the bottom oil of the fractionating tower with the bottom oil of the stripping tower; the stripping bottom oil pump 21 can be not increased, and the original stripping bottom oil pump 16 can be used.
(4) Suitably increase H2S stripping the dry point of the overhead liquid fraction to distill as much as possible of the small diesel fraction carried along with the hot low-fraction oil.
After the improved method of the embodiment is adopted, the operation condition and the energy-saving effect of the residual oil hydrofining device are as follows:
(1) stopping the fractionating tower to feed the heating furnace 11, saving the effective heat load of the heating furnace at 3504kw, which is equivalent to reducing the standard fuel oil by about 354 kg/h; the fractionating tower 12 is stopped, and 7.06t/h of stripping steam of 1.0Mpag at the bottom of the tower and 7021kw of cooling load at the top of the tower are saved (the consumption of circulating cooling water is reduced by 750t/h by 8 ℃ temperature difference equivalent).
(2)H229kg/H of gas discharged from a liquid separation tank at the top of the S stripping tower is reduced by 5.2kg/H compared with the comparative example of 34.2kg/H, which shows that the embodiment can ensure H2Separation requirements of the S stripper.
(3)H2216.2t/H of bottom oil of the S stripping tower is increased by 1.6t/H compared with 214.6t/H of a comparative example, and H2The S content meets the requirements.
(4) After the raw material exchanges heat with the bottom oil of the stripping tower through the heat exchanger 15, the temperature is 278.7 ℃, which is 6.7 ℃ higher than the comparative example of 272 ℃, and the consumption of the standard fuel oil of the reaction feeding heating furnace is correspondingly reduced by about 125 kg/h.
(5) With H2Compared with the comparative example, the diesel fraction of the S stripping tower bottom oil to the catalytic cracking unit is increased by only 1.6t/h, which shows that the material balance of the new flow path is basically the same as that of the comparative example.
(6) The cold low oil flow of the hydrofining device of gasoline and diesel oil fed with unstable naphtha is small and is only 10.4t/h, and the operation of the hydrofining device of gasoline and diesel oil is not influenced.
In conclusion, the embodiment of the invention can firstly ensure the separation requirement of the stripping tower and does not influence the quality and yield of the refined residual oil; and secondly, the fractionating tower system is stopped, so that the flow and the operation are greatly simplified, and the energy consumption is greatly reduced.
The above embodiments are preferred embodiments of the present invention, but the present invention is not limited to the above embodiments, and any other changes, modifications, substitutions, combinations, and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents thereof, and all such changes, modifications, substitutions, combinations, and simplifications are intended to be included in the scope of the present invention.
Claims (3)
1. A residual oil hydrofining process for stopping and starting a fractionating tower system and changing the cold low fraction oil going direction is characterized by comprising the following steps:
(1) the cold low-temperature oil discharged from the cold low-temperature oil separating tank does not enter H any more after being subjected to heat exchange with the hot low-temperature gas separating through the cold low-temperature oil separating primary-hot low-temperature gas separating primary heat exchanger2The S stripping tower is cooled by circulating water through a cooler and then is mixed with H2Mixing unstable naphthas at the top of the stripping tower, and feeding the mixed naphthas to a gasoline and diesel oil hydrofining device for separation;
(2) shutdown H2The fractionating tower system after the S stripping tower comprises a fractionating tower feeding heating furnace, a fractionating tower, a side line diesel stripping tower bottom reboiler, a fractionating tower bottom oil pump, a fractionating tower top oil-gas-hot water heat exchanger, a fractionating tower top oil-gas secondary air cooling, a fractionating tower top oil-gas separation tank, a fractionating tower top cold reflux and a naphtha pump, wherein a raw material primary heat exchanger is reserved, and H is newly added2Pipeline from the bottom oil of S stripping tower to the primary heat exchanger of raw material to make H2And the bottom oil of the S stripping tower directly enters the primary raw material heat exchanger to heat the raw materials.
2. A residue hydrofinishing scheme for a stop-start fractionator system and change of cold low cut oil to the distillate of claim 1, wherein: the cooling by the circulating water in the step (1) means cooling to 40 ℃.
3. A residue hydrofinishing scheme for a stop-start fractionator system and change of cold low cut oil to the distillate of claim 1, wherein: step by stepThe hydrogen atom in step (2)2And a stripping tower bottom oil pump is arranged on a pipeline from the bottom oil of the S stripping tower to the primary raw material heat exchanger, and the stripping tower bottom oil pump is a fractionating tower bottom oil pump of the original shutdown fractionating tower system.
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| CN111394125A (en) * | 2020-04-15 | 2020-07-10 | 上海优华系统集成技术股份有限公司 | Fractionation system and fractionation method of gasoline and diesel hydrogenation device |
| CN113943588B (en) * | 2020-07-16 | 2022-12-02 | 中国石油化工股份有限公司 | Naphtha fractionation process after pre-hydrogenation treatment of continuous reforming device |
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| JP2000273467A (en) * | 1998-10-30 | 2000-10-03 | Jgc Corp | Gas turbine fuel oil and its production and power generation |
| WO2002026917A1 (en) * | 2000-09-26 | 2002-04-04 | Uop Llc | Hydrocracking process |
| CN103497782A (en) * | 2013-10-16 | 2014-01-08 | 黑龙江省能源环境研究院 | Method of producing low-sulfur low freezing point diesel by full-range shale oil |
| CN105838418A (en) * | 2016-06-13 | 2016-08-10 | 黑龙江省能源环境研究院 | Method for improving shale oil hydrorefining denitrification rate |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2000273467A (en) * | 1998-10-30 | 2000-10-03 | Jgc Corp | Gas turbine fuel oil and its production and power generation |
| WO2002026917A1 (en) * | 2000-09-26 | 2002-04-04 | Uop Llc | Hydrocracking process |
| CN103497782A (en) * | 2013-10-16 | 2014-01-08 | 黑龙江省能源环境研究院 | Method of producing low-sulfur low freezing point diesel by full-range shale oil |
| CN105838418A (en) * | 2016-06-13 | 2016-08-10 | 黑龙江省能源环境研究院 | Method for improving shale oil hydrorefining denitrification rate |
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