CN115193340B - Device and method for heating feed for cracking gasoline hydrogenation reaction - Google Patents
Device and method for heating feed for cracking gasoline hydrogenation reaction Download PDFInfo
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- CN115193340B CN115193340B CN202110385972.7A CN202110385972A CN115193340B CN 115193340 B CN115193340 B CN 115193340B CN 202110385972 A CN202110385972 A CN 202110385972A CN 115193340 B CN115193340 B CN 115193340B
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- 238000005984 hydrogenation reaction Methods 0.000 title claims abstract description 114
- 238000010438 heat treatment Methods 0.000 title claims abstract description 41
- 239000003502 gasoline Substances 0.000 title claims abstract description 34
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000005336 cracking Methods 0.000 title 1
- 230000001105 regulatory effect Effects 0.000 claims abstract description 38
- 238000000197 pyrolysis Methods 0.000 claims abstract description 32
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 5
- 239000013589 supplement Substances 0.000 claims description 7
- 238000007670 refining Methods 0.000 abstract description 2
- 239000000126 substance Substances 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 description 20
- 238000006243 chemical reaction Methods 0.000 description 10
- 239000002737 fuel gas Substances 0.000 description 7
- 239000000463 material Substances 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 230000001276 controlling effect Effects 0.000 description 4
- 239000003546 flue gas Substances 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 125000005842 heteroatom Chemical group 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010574 gas phase reaction Methods 0.000 description 1
- 239000004922 lacquer Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J4/00—Feed or outlet devices; Feed or outlet control devices
- B01J4/008—Feed or outlet control devices
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
-
- 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
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/72—Controlling or regulating
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/002—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices the feeding side being of particular interest
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2204/00—Aspects relating to feed or outlet devices; Regulating devices for feed or outlet devices
- B01J2204/007—Aspects relating to the heat-exchange of the feed or outlet devices
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
本发明属于炼油化工技术领域，公开了一种裂解汽油加氢反应进料加热的装置及方法，该装置包括进料加热器，加氢反应器的出料管线上设有进出料换热器，加氢反应进料管线通过进出料换热器与进料加热器的进料口相连，进料加热器的出料口与加氢反应器的进料口相连，进料加热器的蒸汽侧入口与高压蒸汽管线相连，高压蒸汽管线上并联设有一大一小两个调节阀，进料加热器的蒸汽侧出口通过二次蒸汽管线与分离系统的再沸器蒸汽管线相连，所述分离系统上游的二次蒸汽管线上连通有中压蒸汽总管。该装置和方法既能满足加氢反应进料的温度要求，环保且可灵活调节。
The invention belongs to the technical field of oil refining and chemical industry, and discloses a device and method for heating a pyrolysis gasoline hydrogenation reaction feed, the device comprises a feed heater, a feed inlet and a feed outlet heat exchanger is arranged on the discharge pipeline of the hydrogenation reactor, the hydrogenation reaction feed pipeline is connected to the feed inlet of the feed heater through the feed inlet and a feed outlet heat exchanger, the discharge inlet of the feed heater is connected to the feed inlet of the hydrogenation reactor, the steam side inlet of the feed heater is connected to the high-pressure steam pipeline, two regulating valves, one large and one small, are arranged in parallel on the high-pressure steam pipeline, the steam side outlet of the feed heater is connected to the reboiler steam pipeline of the separation system through the secondary steam pipeline, and the secondary steam pipeline upstream of the separation system is connected to a medium-pressure steam main pipe. The device and method can meet the temperature requirements of the hydrogenation reaction feed, are environmentally friendly and can be flexibly adjusted.
Description
Technical Field
The invention belongs to the technical field of oil refining and chemical industry, and particularly relates to a device and a method for heating pyrolysis gasoline hydrogenation reaction feed.
Background
Pyrolysis gasoline (also known as "heavy pyrolysis gasoline (pygas)") is a liquid byproduct of the steam cracking process for producing ethylene and propylene. Pyrolysis gasoline is a highly unsaturated hydrocarbon mixture (carbon range about C5-C14) rich in dienes, olefins, and aromatics, especially benzene, while pyrolysis gasoline also includes heteroatom-containing hydrocarbons such as sulfur and nitrogen-containing compounds. If pyrolysis gasoline is untreated, it is typically degraded in fuel systems to produce gums and lacquers. In order to increase the utility value of pyrolysis gasoline, which must be at least partially hydrogenated or hydrotreated to reduce the unsaturation and heteroatom-containing hydrocarbon content, so that it can be used as a gasoline blending stock.
The hydrogenation saturation and desulfurization of pyrolysis gasoline are gas phase reactions. According to the chemical reaction principle, the unsaturated hydrocarbon is hydrogenated into an exothermic reaction. The existing pyrolysis gasoline hydrogenation device is provided with a feeding and discharging heat exchanger and a heating furnace at the inlet of the gas phase reactor, the feeding and discharging heat exchanger is used for recovering hydrogenation reaction heat release, and the heating furnace ensures that the hydrogenation reaction feeding temperature reaches the initial temperature required by the reaction. In the initial stage of device operation, the hydrogenation reaction is not started yet, the heat release amount of the reaction is small, the heat load of the heating furnace is high, when the normal reaction temperature is reached, the heat release amount of the hydrogenation reaction is increased, the heat of the reaction is efficiently recovered by the feeding and discharging heat exchanger, the external supplementary heat required by the system is reduced, and the heat load of the heating furnace is reduced. However, the heating furnace does not have the characteristic of low load adjustment, so that when the heat load is low and the fuel gas flow is small, the burner of the heating furnace is easy to flameout, and serious potential safety hazard is brought to the device. Meanwhile, in the combustion process of the fuel gas, sulfur-containing and carbon dioxide-containing flue gas can be generated, and the flue gas is directly discharged to cause environmental pollution.
Patent document CN104560161a discloses a method for heating the material at the inlet of a second-stage reactor of a pyrolysis gasoline hydrogenation unit, wherein the second-stage feeding is heated by high-pressure steam without using a heating furnace. The operation pressure of the high-pressure steam heat exchanger is more than 6.0MPaG, the material is heated by utilizing the condensation latent heat of the high-pressure steam, the operation pressure is high, and the safety is low. The utilization of the latent heat of condensation to heat the material is unfavorable for the adjustment in low load, and the operation is inflexible.
Disclosure of Invention
Aiming at the problems existing in the prior art, the invention aims to provide a device and a method for heating the feeding material in the pyrolysis gasoline hydrogenation reaction, which not only meet the environmental protection requirement, but also ensure flexible and reliable adjustment according to the use characteristics of a feeding heater.
The invention provides a device for heating pyrolysis gasoline hydrogenation reaction feed, which comprises a hydrogenation reactor and a separation system, wherein a discharge pipeline of the hydrogenation reactor is provided with a feed-in and discharge heat exchanger, a hydrogenation reaction feed pipeline is connected with a feed inlet of the feed heater through the feed-in and discharge heat exchanger, a discharge port of the feed heater is connected with the feed inlet of the hydrogenation reactor, a steam side inlet of the feed heater is connected with a high-pressure steam pipeline, a large regulating valve and a small regulating valve are arranged on the high-pressure steam pipeline in parallel, a steam side outlet of the feed heater is connected with a reboiler steam pipeline of the separation system through a secondary steam pipeline, and a secondary steam pipeline at the upstream of the separation system is communicated with a medium-pressure steam header pipe.
In a second aspect, the present invention provides a process for heating a pyrolysis gasoline hydrogenation reaction feed using the apparatus described above, the process comprising:
1) Introducing medium-pressure steam through a secondary steam pipeline, preheating a feed heater and a steam side pipeline thereof, introducing high-pressure steam through a high-pressure steam pipeline, heating hydrogenation reaction feed through the feed heater, decompressing the high-pressure steam through a regulating valve on the high-pressure steam pipeline, controlling steam flow, and taking secondary steam at a steam side outlet of the feed heater as a supplementary heat source of a separation system;
2) After the hydrotreatment device runs stably, if the temperature rise of the hydrogenation reaction is lower, the temperature of the hydrogenation reaction feed is lower than the hydrogenation reaction temperature after passing through the feed-in and feed-out heat exchanger, the temperature switch for adjusting the opening of the bypass adjusting valve of the feed-in and feed-out heat exchanger is adjusted to the cold side outlet temperature of the feed-in heat exchanger, the temperature of the hydrogenation reaction feed is controlled by adjusting the size adjusting valve on the high-pressure steam pipeline, the feed heater supplements heat for the system, and if the temperature rise of the hydrogenation reaction is higher, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the feed-in and feed-out heat exchanger, the temperature switch for adjusting the opening of the bypass adjusting valve of the feed-in and feed-out heat exchanger is adjusted to the feed inlet temperature of the hydrogenation reactor, and the feed heater is deactivated.
Compared with the prior art, the invention has the following advantages:
(1) According to the invention, the feeding heater using steam as a heat source is adopted to replace the existing heating furnace to heat hydrogenation reaction feeding, meanwhile, the defects of overhigh operation pressure, poor safety, poor regulation performance and the like of the feeding heater are avoided, timely response and stable regulation of process fluctuation are realized, the operation safety is improved, the environment-friendly index of the device is improved, the high-load external heat supplement can be realized to meet the driving requirement of the device, the continuous operation of small-load heat supply can be realized, the zero smoke emission and low-carbon environment-friendly operation of the device are realized, and the device is more green and environment-friendly.
(2) The high-temperature steam after decompression is adopted in the feeding heater, the sensible heat of the steam is utilized to heat hydrogenation reaction feeding, the steam consumption can be adjusted by 0-Fmax, the adjusting range is wide, the difficulty that the fuel gas of the heating furnace cannot be adjusted by 0-Fmax in a low limit is overcome, and the flexibility and the safety of the operation of the device are improved.
(3) The invention carries out continuous twice heat utilization on steam, namely, the once heat utilization takes the sensible heat of the steam to heat hydrogenation reaction feeding, the regulating valve precisely controls the steam consumption and regulates the reaction feeding temperature, the used secondary steam enters the separation system again, the latent heat of the steam is taken to heat the materials of the separation system, and finally the generated steam condensate is discharged out of the device, and the twice heat utilization not only meets the heat requirement of high temperature, but also fully recovers the heat value of the steam, and keeps the advancement of the energy consumption of the device.
(4) The device and the method not only ensure the requirement that the hydrogenation reaction feeding needs to supplement heat to feed a heater with higher heat load in the device starting stage, but also solve the difficult problem of low-load heat supplement adjustment when the hydrogenation reaction is unstable in heat release and improve the stability and safety of the device operation.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate the invention and together with the description serve to explain, without limitation, the invention.
FIG. 1 is a schematic process flow diagram of an apparatus for heating a pyrolysis gasoline hydrogenation reaction feed according to one embodiment of the present invention.
FIG. 2 is a schematic process flow diagram of a pyrolysis gasoline hydrogenation reaction feed heating device used in the prior art.
Description of the reference numerals
The device comprises a feeding heat exchanger, a discharging heat exchanger, a feeding heater, a hydrogenation reactor, a4 drainage valve group, a 5 separation system, a 6 heating furnace, an S-1 hydrogenation reaction feeding pipeline, an S-2 high-pressure steam pipeline, an S-3 secondary steam pipeline, an S-4 steam condensate pipeline, an S-5 steam condensate discharge pipeline, an S-6 fuel gas pipeline and an S-7 medium-pressure steam header pipe.
Detailed Description
In order that the invention may be more readily understood, the invention will be described in detail below with reference to the following examples and the accompanying drawings, which are given by way of illustration only and are not intended to be limiting.
According to a first aspect of the invention, the invention provides a pyrolysis gasoline hydrogenation reaction feed heating device, the pyrolysis gasoline hydrogenation treatment device comprises a hydrogenation reactor and a separation system, the device comprises a feed heater, a feed-in and feed-out heat exchanger is arranged on a discharge pipeline of the hydrogenation reactor, a hydrogenation reaction feed pipeline is connected with a feed inlet of the feed heater through the feed-in and feed-out heat exchanger, a discharge port of the feed heater is connected with the feed inlet of the hydrogenation reactor, a steam side inlet of the feed heater is connected with a high-pressure steam pipeline, a large regulating valve and a small regulating valve are arranged on the high-pressure steam pipeline in parallel, a steam side outlet of the feed heater is connected with a reboiler steam pipeline of the separation system through a secondary steam pipeline, and a medium-pressure steam header pipe is communicated with the secondary steam pipeline at the upstream of the separation system.
According to the invention, the large regulating valve is used for regulating the flow when the steam consumption is high, in particular, the large regulating valve is used for regulating the flow in the startup stage of the hydrogenation reactor, the small regulating valve is used for regulating the flow under the working condition of low steam consumption, in particular, the working condition that a small amount of heat is required to be supplemented under the normal operation of the hydrogenation reactor.
According to the invention, a bypass regulating valve of the feeding and discharging heat exchanger is arranged on a discharging pipeline of the hydrogenation reactor, the feeding and discharging heat exchanger is connected with the bypass regulating valve of the feeding and discharging heat exchanger in parallel, and the opening of the bypass regulating valve of the feeding and discharging heat exchanger is regulated by selecting the outlet temperature of the cold side of the feeding and discharging heat exchanger or the temperature of the feeding inlet of the hydrogenation reactor through a temperature switch.
Preferably, the opening of the regulating valve on the high-pressure steam pipeline is regulated by the hydrogenation reaction feed temperature of the cold side outlet of the feed heater.
Preferably, the steam side outlet of the feed heater is provided with a condensate draining pipeline connected with the secondary steam pipeline in parallel, and the condensate draining pipeline is connected with the steam condensate pipeline through a drain valve group. The secondary steam pipeline is arranged to use the secondary steam of the high-pressure steam as a supplementary heat source for the separation system in the device. The setting of the condensate draining pipeline is that medium-pressure steam is introduced to preheat and drain the steam side equipment and pipelines in the driving stage. In addition, the medium pressure steam outlet of the medium pressure steam main pipe is positioned between the separation system and the condensate inlet of the condensate draining pipeline and is close to the separation system, the medium pressure steam is supplied by the medium pressure steam main pipe communicated with the secondary steam pipeline, and the flowing direction of the medium pressure steam is opposite to that of the secondary steam in the preheating stage, so that a one-way valve connected in parallel with a valve for controlling the flowing direction of the secondary steam on the secondary steam pipeline can be arranged to control the flowing direction of the medium pressure steam.
In the invention, a steam condensate discharge pipeline is arranged on the separation system.
The system components which are not limited in the invention can be selected conventionally according to the prior art, and belong to conventional technical means, such as valves arranged on a condensate draining pipeline and a secondary steam pipeline.
According to a second aspect of the present invention there is provided a process for heating a pyrolysis gasoline hydrogenation reaction feed using the apparatus described above, the process comprising:
1) Introducing medium-pressure steam through a secondary steam pipeline, preheating a feed heater and a steam side pipeline thereof, introducing high-pressure steam through a high-pressure steam pipeline, heating hydrogenation reaction feed through the feed heater, decompressing the high-pressure steam through a regulating valve on the high-pressure steam pipeline, controlling steam flow, and taking secondary steam at a steam side outlet of the feed heater as a supplementary heat source of a separation system;
2) After the hydrotreatment device runs stably, if the temperature rise of the hydrogenation reaction is lower, the temperature of the hydrogenation reaction feed is lower than the hydrogenation reaction temperature after passing through the feed-in and feed-out heat exchanger, the temperature switch for adjusting the opening of the bypass adjusting valve of the feed-in and feed-out heat exchanger is adjusted to the cold side outlet temperature of the feed-in heat exchanger, the temperature of the hydrogenation reaction feed is controlled by adjusting the size adjusting valve on the high-pressure steam pipeline, the feed heater supplements heat for the system, and if the temperature rise of the hydrogenation reaction is higher, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the feed-in and feed-out heat exchanger, the temperature switch for adjusting the opening of the bypass adjusting valve of the feed-in and feed-out heat exchanger is adjusted to the feed inlet temperature of the hydrogenation reactor, and the feed heater is deactivated.
According to the invention, the medium pressure steam has a temperature of 150-300 ℃ and a pressure of 1.0-1.8MPaG. The medium pressure steam is introduced to preheat the feed heater and its steam side line.
Preferably, the high pressure steam has a temperature of 320-420 ℃ and a pressure of greater than 2.0MPaG.
Preferably, the feed heater vapor side is operated at a pressure of 1.0 to 1.8MPaG.
Preferably, the pressure of the secondary steam is 1.0-1.8MPaG, and the temperature of the secondary steam is at least 10 ℃ above the saturation temperature at the corresponding pressure.
In the present invention, the hydrogenation reaction temperature may be 200 to 350 ℃.
The process parameters not defined in the present invention can be set conventionally according to the prior art.
The following describes the invention in detail by way of examples.
Examples
This example is illustrative of the apparatus and method of the present invention for heating a pyrolysis gasoline hydrogenation feed.
As shown in fig. 1, the invention provides a pyrolysis gasoline hydrogenation reaction feeding heating device, which comprises a feeding heater 2, wherein a feeding and discharging heat exchanger 1 is arranged on a discharging pipeline of a hydrogenation reactor 3, a hydrogenation reaction feeding pipeline S-1 is connected with a feeding port of the feeding heater 2 through the feeding and discharging heat exchanger 1, a discharging port of the feeding heater 2 is connected with a feeding port of the hydrogenation reactor 3, a steam side inlet of the feeding heater 2 is connected with a high-pressure steam pipeline S-2, a large regulating valve and a small regulating valve are arranged on the high-pressure steam pipeline S-2 in parallel, a steam side outlet of the feeding heater 2 is connected with a reboiler steam pipeline of a separation system 5 through a secondary steam pipeline S-3, and a secondary steam pipeline S-3 at the upstream of the separation system 5 is communicated with a medium-pressure steam main pipe S-7.
The discharge pipeline of the hydrogenation reactor 3 is provided with a feed and discharge heat exchanger bypass regulating valve, the feed and discharge heat exchanger 1 and the feed and discharge heat exchanger bypass regulating valve are arranged in parallel, and the opening of the feed and discharge heat exchanger bypass regulating valve is regulated by selecting the outlet temperature of the cold side of the feed and discharge heat exchanger 1 or the temperature of the feed inlet of the hydrogenation reactor 3 through a temperature switch. The opening of the regulating valve on the high-pressure steam pipeline S-2 is regulated by the hydrogenation reaction feeding temperature of the cold side outlet of the feeding heater 2. The steam side outlet of the feeding heater 2 is provided with a condensate draining pipeline connected with the secondary steam pipeline S-3 in parallel, and the condensate draining pipeline is connected with the steam condensate pipeline S-4 through a drain valve group 4. The separation system 5 is provided with a steam condensate discharge pipeline S-5.
Taking a 40 ten thousand ton/year pyrolysis gasoline hydrogenation device as an example, the method for heating pyrolysis gasoline hydrogenation reaction feed by adopting the device comprises the following steps:
1) The hydrogenation reaction starting stage comprises the steps of firstly introducing medium-pressure steam through a secondary steam pipeline S-3, preheating a feed heater 2 and a steam side pipeline thereof, introducing high-pressure steam through a high-pressure steam pipeline S-2, wherein the temperature of the high-pressure steam is 420 ℃, the pressure of the high-pressure steam is 3.4MPaG, heating hydrogenation reaction feed through the feed heater 2, the operating pressure of the steam side of the feed heater is 1.35MPaG, the operating temperature is 406 ℃, decompressing the high-pressure steam through a regulating valve on the high-pressure steam pipeline S-2, controlling the steam flow, guaranteeing the hydrogenation reaction feed temperature, taking secondary steam at the steam side outlet of the feed heater 2 as a supplementary heat source of a separation system 5, the pressure of the secondary steam is 1.3MPaG, and the temperature of the secondary steam is 280 ℃;
2) After the hydrotreatment device runs stably, if the temperature rise of the hydrogenation reaction is lower, the temperature of the hydrogenation reaction feed is lower than the hydrogenation reaction temperature after passing through the feeding and discharging heat exchanger 1, the hydrogenation reaction temperature is 240 ℃, a temperature switch for adjusting the opening of a bypass adjusting valve of the feeding and discharging heat exchanger is adjusted to the outlet temperature of the cold side of the feeding and discharging heat exchanger 1, the temperature of the hydrogenation reaction feed is controlled by adjusting a size adjusting valve on a high-pressure steam pipeline S-2, the feeding heater 2 supplements heat for a system, and if the temperature rise of the hydrogenation reaction is higher, the temperature of the hydrogenation reaction feed can reach the hydrogenation reaction temperature after passing through the feeding and discharging heat exchanger, the temperature switch for adjusting the opening of the bypass adjusting valve of the feeding and discharging heat exchanger is adjusted to the temperature of a feed inlet of the hydrogenation reactor 3, and the feeding heater 2 is deactivated.
Comparative example
As shown in FIG. 2, a pyrolysis gasoline hydrogenation reaction feed heating device is adopted in the industry in the prior art, and a heating furnace 6 is adopted for heating the feed in a hydrogenation reaction feed line S-1.
In the initial stage of device operation, the hydrogenation reaction in the hydrogenation reactor 3 is not started yet, the reaction heat release amount is small, the heat load of the heating furnace 6 is higher, when the normal reaction temperature is reached, the hydrogenation reaction heat release amount is increased, the feeding and discharging heat exchanger 1 efficiently recovers the reaction heat, the external supplementary heat required by the system is reduced, and the heat load of the heating furnace 6 is reduced. However, since the heating furnace 6 does not have the low-load regulation characteristic, when the heat load is low, the burner of the heating furnace is easy to flameout when the fuel gas flow in the fuel gas pipeline S-6 is small, and serious potential safety hazard is brought to the device. Meanwhile, in the combustion process of the fuel gas, sulfur-containing and carbon dioxide-containing flue gas can be generated, and the flue gas is directly discharged to cause environmental pollution.
The comparison of the characteristics of the examples and comparative examples is shown in Table 1.
TABLE 1
The embodiments of the present invention have been described above, the description is illustrative, not exhaustive, and not limited to the disclosed embodiments. Many modifications and variations will be apparent to those of ordinary skill in the art without departing from the scope and spirit of the described embodiments.
Claims (5)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110385972.7A CN115193340B (en) | 2021-04-09 | 2021-04-09 | Device and method for heating feed for cracking gasoline hydrogenation reaction |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202110385972.7A CN115193340B (en) | 2021-04-09 | 2021-04-09 | Device and method for heating feed for cracking gasoline hydrogenation reaction |
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| Publication Number | Publication Date |
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| CN115193340A CN115193340A (en) | 2022-10-18 |
| CN115193340B true CN115193340B (en) | 2025-03-25 |
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| CN203790604U (en) * | 2014-05-07 | 2014-08-27 | 大庆中蓝石化有限公司 | Secondary flash steam recycling and reusing system of C4 separation device |
| CN107937022A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | Pyrolysis gasoline hydrogenation device and method |
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| CN104560161A (en) * | 2015-02-05 | 2015-04-29 | 中石化上海工程有限公司 | Method for heating materials at inlet of second-stage reactor of pyrolysis gasoline hydrogenation device |
| CN207091361U (en) * | 2017-06-29 | 2018-03-13 | 中国石油天然气集团公司 | A kind of reaction heating system for gasoline hydrogenation reaction |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN203790604U (en) * | 2014-05-07 | 2014-08-27 | 大庆中蓝石化有限公司 | Secondary flash steam recycling and reusing system of C4 separation device |
| CN107937022A (en) * | 2017-11-21 | 2018-04-20 | 宁波东鼎石化装备有限公司 | Pyrolysis gasoline hydrogenation device and method |
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