CN105670689A - Kerosene-hydrogenation production process and system - Google Patents
Kerosene-hydrogenation production process and system Download PDFInfo
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- CN105670689A CN105670689A CN201610069300.4A CN201610069300A CN105670689A CN 105670689 A CN105670689 A CN 105670689A CN 201610069300 A CN201610069300 A CN 201610069300A CN 105670689 A CN105670689 A CN 105670689A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/14—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including at least two different refining steps in the absence of hydrogen
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kerosene-hydrogenation production process. The process comprises a reaction part and a fractionation part, wherein a reaction product of the reaction part directly enters a high-pressure hot separator without being cooled after exchanging heat with raw materials, a flash steam phase is cooled to about 50 DEG C through an air cooler after exchanging heat with recycle hydrogen or new hydrogen and then enters a high-pressure cold separator, and high-temperature reaction products separated from the bottoms of the high-pressure hot separator and the high-pressure cold separator exchange heat with refined kerosene from the bottom of a fractionating tower and are sent to the fractionation part. Compared with the prior art, the kerosene-hydrogenation production process is improved, the energy recycle efficiency of a device can be effectively improved and the energy consumption of the device is reduced with the process. The invention further provides a kerosene-hydrogenation production system adopting the kerosene-hydrogenation production process.
Description
Technical field
The present invention relates to the production technology of a kind of kerosene hydrogenation, hydrogenated refining by coal that straight run is navigated, produce the low-sulfur boat coal meeting jet fuel standard.
Background technology
Jet fuel, also known as aerial kerosene, is called for short boat coal, is widely used in military aircraft and aircarrier aircraft. The kerosene distillate that its production method is usually normal pressure one line straight-run fuel oil or secondary operations obtain obtains through deep hydrofinishing.
Hydrofinishing can remove the non-hydrocarbons such as the sulfur in fuel oil, oxygen, nitrogen effectively, and some olefin, aromatic hydrogenation can be made saturated. According to the difference adopting catalyst system, its operating condition is generally at temperature 200～400 DEG C, pressure 0.7～3.2MPa, air speed 2～4h-1, hydrogen-oil ratio 30～200.
Industrial typical kerosene hydrogenation processing technological flow at present is shown in accompanying drawing 7,8,9,10, is typically based on practical situation and selects different technological processes.
1. the mixed hydrogen flow process (see accompanying drawing 7) of furnace rear
After boat coal raw material is pressurized, first after heat exchanger E1 with product heat exchange, enter raw materials furnace and heating F1 heating, then mix with from recycle hydrogen, enter boat coal desulfurization alcohol reactor R1.
Product out, is introduced into heat exchanger E1 and raw material heat exchange bottom sweetening reaction device R1, enters cold high pressure separator D1 after being cooled to about 50 DEG C then through air cooler E2 and water cooler E3. Oil-gas Separation in cold high pressure separator D1, tank deck oil gas buffered tank D2 enters circulating hydrogen compressor K1 after supplementing new hydrogen, it is sent to the preheating of heating furnace convection section by compressor pressurization, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enters boat coal desulfurization alcohol reactor R1.
Owing to course of reaction hydrogen consumption is low, hydrogen purity change is little, cold high pressure separator D1 the tail hydrogen discharged can directly be discharged into low pressure hydrogen pipe network after treatment and be continuing with, and the hydrogen needed for reaction is once passed through by new hydrogen, directly provides. It is specifically shown in mixed the hydrogen flow process of hydrogen of accompanying drawing 9 furnace rear.
By the low-temperature oil discharged bottom cold high pressure separator D1, after heat exchanger E4 heat exchange, enter fractionating column C1 with the refining boat product of coal from fractionation column base.
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower.Heat at the bottom of tower is provided by reboiler furnace F2. At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
2. the mixed hydrogen recycle hydrogen flow process (see accompanying drawing 8) in stokehold
Boat coal raw material is pressurized mix with hydrogen after, first after heat exchanger E1 with product heat exchange, enter back into raw materials furnace and heating F1 heating, enter the coal desulfurization alcohol reactor R1 that navigates.
Product out, is introduced into heat exchanger E1 and raw material heat exchange bottom boat coal desulfurization alcohol reactor R1, enters cold high pressure separator D1 after being cooled to about 50 DEG C then through air cooler E2 and water cooler E3. Oil-gas Separation in cold high pressure separator D1, tank deck oil gas buffered tank D2 enters circulating hydrogen compressor K1 after supplementing new hydrogen, compressor pressurization be sent to the preheating of heating furnace convection section, enters heat exchanger E1 with raw oil after heat exchanger E1 entrance mixes.
Owing to course of reaction hydrogen consumption is low, hydrogen purity change is little, cold high pressure separator D1 the tail hydrogen discharged can directly be discharged into low pressure hydrogen pipe network after treatment and be continuing with, and the hydrogen needed for reaction is once passed through by new hydrogen, directly provides. It is specifically shown in mixed the hydrogen flow process of hydrogen in accompanying drawing 10 stokehold.
By the low-temperature oil discharged bottom cold high pressure separator D1, after heat exchanger E4 heat exchange, enter fractionating column C1 with the refining boat product of coal from fractionation column base.
Fractionating column part flow process is identical with the mixed hydrogen flow process of furnace rear.
The deficiency of several technological processes is in that above: owing to have employed cold high split flow, and material is repeated cooling and heating, causes that device energy regenerating utilization rate is low, and energy consumption is higher.
Summary of the invention
It is an object of the invention to provide the kerosene hydrogenation technique of a kind of improvement, adopt this technique can be effectively improved device energy regenerating utilization ratio, reduce plant energy consumption.
The purpose of the present invention implements by the following technical programs:
A kind of production technology of kerosene hydrogenation, including reactive moieties and fractionating section, the product of described reactive moieties with boat coal raw material heat exchange after not cooled, it is directly entered high pressure hot separator, it is cooled to 45-55 DEG C through air cooler after the vapour phase flashed off and recycle hydrogen or new hydrogen heat exchange, be preferably after 50 DEG C and enter cold high pressure separator, by the high-temperature reaction product separated bottom high pressure hot separator and cold high pressure separator with after the refining boat coal heat exchange of Fractionator Bottom, send into fractionating section.
Further, the product of described reactive moieties and boat coal raw material heat exchange, including after the boat product of coal fractionated out from fractionating section and fractionating column charging heat exchange, as heat source medium and the boat further heat exchange of coal raw material.
Further, the production technology of described kerosene hydrogenation includes four kinds of technological processes: the mixed hydrogen of furnace rear adds raw produce heat exchange process, the mixed hydrogen in stokehold adds raw produce heat exchange process, the mixed hydrogen flow process of the mixed hydrogen flow process of furnace rear or stokehold.
Preferably, described furnace rear mixed hydrogen includes following operation when adding raw produce heat exchange process:
(1) reactive moieties
After boat coal raw material pressurization, first boat product of coal heat exchange in heat exchanger E9 and from the hot side outlet of heat exchanger E4, after heat exchanger E1 and product heat exchange, enter raw materials furnace and heating F1 heating, after heating raw materials outlet of still mixes with recycle hydrogen, enter boat coal desulfurization alcohol reactor R1;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, it is sent in heat exchanger E3 by circulating hydrogen compressor pressurization and after the oil gas heat exchange of high pressure hot separator, enter the preheating of raw materials furnace and heating convection section, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enter boat coal desulfurization alcohol reactor R1;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower; Heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, then through heat exchanger E9 and the further heat exchange of raw material, is cooled to less than 45 DEG C through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal after.
Preferably, the mixed hydrogen in described stokehold includes following operation when adding raw produce heat exchange process:
(1) reactive moieties
Boat coal raw material is pressurized and after mixing with recycle hydrogen, first boat product of coal heat exchange in heat exchanger E9 and from the hot side outlet of heat exchanger E4, after heat exchanger E1 and product heat exchange, enter raw materials furnace and heating F1 heating, subsequently into boat coal desulfurization alcohol reactor R1;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after then mixing with raw oil, enter heat exchanger E1 and product heat exchange;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower;Heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, then through heat exchanger E9 and the further heat exchange of raw material, is cooled to less than 45 DEG C through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal after.
Preferably, described furnace rear includes following operation when mixing hydrogen flow process:
(1) reactive moieties
After boat coal raw material is pressurized, first through in heat exchanger E1 with product heat exchange after, enter raw materials furnace and heating F1 heating, then mix with recycle hydrogen, enter the coal desulfurization alcohol reactor R1 that navigates;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enter boat coal desulfurization alcohol reactor R1;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, and by obtaining refining boat coal at the bottom of tower, heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
Preferably, described stokehold includes following operation when mixing hydrogen flow process:
(1) reactive moieties
Boat coal raw material is pressurized and mix with recycle hydrogen, first through in heat exchanger E1 with product heat exchange after, enter raw materials furnace and heating F1 heating, subsequently into the coal desulfurization alcohol reactor R1 that navigates;
Hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after then mixing with raw oil, enter heat exchanger E1 and product heat exchange;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, and by obtaining refining boat coal at the bottom of tower, heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
Further, being provided with absorption digester R2 on boat product of coal line, described absorption digester R2 is connected with described water cooler E6.
Present invention also offers the production system of a kind of kerosene hydrogenation, it includes the production technology of described kerosene hydrogenation.
The production technology of kerosene hydrogenation of the present invention, compared with conventional art, the present invention provides the kerosene hydrogenation technique of a kind of improvement, adopts this technique can be effectively improved device energy regenerating utilization ratio, reduces plant energy consumption.
After adopting the high pressure hot separator that the present invention proposes to add the high pressure hot separator kerosene hydrogenation technological process of cold high pressure separator, after product and raw material heat exchange not cooled, it is directly entered high pressure hot separator, fractionating column charging heat-exchange system is directly sent by the high-temperature reaction product separated bottom high pressure hot separator, one side can make the cooling load reduction of response system more than 85%, high-temperature hot product makes fractionating column feeding temperature obtain certain raising on the other hand, thus causing that fractionating column reboiler heat duty reduces about 25%. And the vapour phase that high pressure hot separator flashes off and the heat exchange of recycle hydrogen or new hydrogen, then enable and measure with further recovery, directly reduce the thermic load about more than 5% of raw materials furnace and heating.
For further recovery waste heat, the present invention is also additionally arranged the heat exchange of raw material and boat product of coal, has reclaimed the waste heat of boat product of coal on the one hand, on the other hand due to the raising of the coal raw material preheating temperature that navigates so that raw materials furnace and heating thermic load reduces about more than 30%.
After adopting the present invention, the public work of kerosene hydrogenation device cools down load reduction about 30%, and heating load reduces about 30%, and energy-saving effect is notable.
Accompanying drawing explanation
Below according to drawings and Examples, the present invention is described in further detail.
Fig. 1 improves the mixed hydrogen of kerosene hydrogenation device furnace rear to add raw produce heat exchange process schematic diagram.
Fig. 2 improves the mixed hydrogen in kerosene hydrogenation device stokehold to add raw produce heat exchange process schematic diagram.
Fig. 3 improves the mixed hydrogen schematic flow sheet of kerosene hydrogenation device furnace rear.
Fig. 4 improves the mixed hydrogen schematic flow sheet in kerosene hydrogenation device stokehold.
Fig. 5 improves mixed the hydrogen schematic flow sheet of hydrogen of kerosene hydrogenation device furnace rear.
Fig. 6 improves mixed the hydrogen schematic flow sheet of hydrogen in kerosene hydrogenation device stokehold.
Fig. 7 is the mixed hydrogen schematic flow sheet of conventional kerosene hydrogenation device furnace rear.
Fig. 8 is the mixed hydrogen schematic flow sheet in conventional kerosene hydrogenation device stokehold.
Fig. 9 is mixed the hydrogen schematic flow sheet of hydrogen of conventional kerosene hydrogenation device furnace rear.
Figure 10 is mixed the hydrogen schematic flow sheet of hydrogen in conventional kerosene hydrogenation device stokehold.
Detailed description of the invention
The present embodiment adopts the mixed hydrogen high pressure hot separator technique of furnace rear, and technological process is referring to accompanying drawing 1.
(1) reactive moieties
Boat coal raw material S1 (40 DEG C after pressurized, 166 ton hour), first in heat exchanger E9 and the boat product of coal S30 heat exchange from the hot side outlet of heat exchanger E4 extremely about 138 DEG C, then through heat exchanger E1 and product S5 heat exchange to after 251 DEG C, raw materials furnace and heating F1 heating is entered to about 272 DEG C via pipeline 2, after mixing with recycle hydrogen S14 again, enter boat coal desulfurization alcohol reactor R1 via pipeline 4.
Boat coal desulfurization alcohol reactor R1 operating condition is 2.0MPa, 260 DEG C, and hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously.
Product S5 temperature 261 DEG C, bottom boat coal desulfurization alcohol reactor R1 out, first after heat exchanger E1 is cooled to 163 DEG C with raw material heat exchange, high pressure hot separator D4 is entered then through by pipeline 6, the vapour phase S7 rich in hydrogen flashed off in high pressure hot separator D4 is first cooled to 126 DEG C through heat exchanger E3 with recycle hydrogen S12 heat exchange, entering air cooler E2 then through by pipeline 8, further condensing cooling is to after about 50 DEG C, entering cold high pressure separator D1 via pipeline 9.
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen H2 rich in the oil gas S10 buffered tank D2 of hydrogen, through being sent to heat exchanger E3 by pipeline 12 after being pressurizeed by compressor, with from high pressure hot separator oil gas S7 heat exchange to after 140 DEG C, the preheating of heating furnace convection section is entered via pipeline 13, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil S3, enter boat coal desulfurization alcohol reactor R1 via pipeline 4.
By high-temperature reaction product S31 and S32 separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 be preheated to 230 DEG C from the refining boat coal S22 heat exchange bottom fractionating column C1 after, send into fractionating column C1.
(2) fractionating column part
Anti-afterproduct S16 after preheated enters the middle part of fractionating column C1, and it is 0.22MPa that fractionating column C1 operates pressure. In fractionating column C1, oil gas S17 rich in hydrogen, hydrogen sulfide is steamed by tower top, after air cooler E7, water cooler E8 condensing cooling are to about 40 DEG C, return tank D3 is entered through pipeline 18, the sour gas S19 being dissolved in the hydrogen in oil, hydrogen sulfide and a small amount of light oil separates from tank top, through pipeline 19 carrying device, a small amount of light oil S20 is through the regular carrying device of pipeline 20. Remaining material S21 all returns tower top via pipeline 21 as backflow.
Be stripped of hydrogen, hydrogen sulfide refining boat coal S22 by extraction at the bottom of tower, first it is cooled to 177 DEG C through heat exchanger E4 with tower charging heat exchange, then it is cooled to 85 DEG C through heat exchanger E9 with the further heat exchange of raw material, finally it is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal. Heat at the bottom of fractionating column C1 tower is provided by reboiler furnace F2.
For guaranteeing boat product of coal quality, being provided with absorption digester R2 on boat product of coal line, described absorption digester R2 is connected with described water cooler E6.
Table 1 gives the thermic load data of each cold exchange device in this technique.
Table 1. is cold changes system heat load summary sheet (kW)
Embodiment 2
The present embodiment adopts the mixed hydrogen high pressure hot separator technique in stokehold, and technological process is referring to accompanying drawing 2.
(1) reactive moieties
Boat coal raw material S1 (40 DEG C, 166 ton hour) after pressurized, first after heat exchanger E9 with the boat product of coal S30 heat exchange from the hot side outlet of heat exchanger E4 extremely about 138 DEG C, mixes through pipeline 29 with recycle hydrogen S14.Liquid-vapor mixture, after heat exchanger E1 and product S5 heat exchange are to 245 DEG C, enter raw materials furnace and heating F1 via pipeline 3 and heats to 260 DEG C, enter boat coal desulfurization alcohol reactor R1 via pipeline 4.
Boat coal desulfurization alcohol reactor R1 operating condition is 2.0MPa, 260 DEG C, and hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously.
Product S5 temperature 261 DEG C, bottom boat coal desulfurization alcohol reactor R1 out, first after heat exchanger E1 is cooled to 164 DEG C with raw material heat exchange, high pressure hot separator D4 is entered then through by pipeline 6, the vapour phase S7 rich in hydrogen flashed off in high pressure hot separator D4 is first cooled to 145 DEG C through heat exchanger E3 with recycle hydrogen S12 heat exchange, entering air cooler E2 then through by pipeline 8, further condensing cooling is to after about 50 DEG C, entering cold high pressure separator D1 via pipeline 9.
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen H2 rich in the oil gas S10 buffered tank D2 of hydrogen, through being sent to heat exchanger E3 by pipeline 12 after being pressurizeed by compressor, with from high pressure hot separator oil gas S7 heat exchange to after 140 DEG C, enter the preheating of heating furnace convection section via pipeline 13, mix before heat exchanger E1 with boat coal raw material S29 then through pipeline 14.
By high-temperature reaction product S31 and S32 separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 be preheated to 229 DEG C from the refining boat coal S22 heat exchange bottom fractionating column C1 after, send into fractionating column C1.
(2) fractionating column part
Anti-afterproduct S16 after preheated enters the middle part of fractionating column C1, and it is 0.22MPa that fractionating column C1 operates pressure. In fractionating column C1, oil gas S17 rich in hydrogen, hydrogen sulfide is steamed by tower top, after air cooler E7, water cooler E8 condensing cooling are to about 40 DEG C, return tank D3 is entered through pipeline 18, the sour gas S19 being dissolved in the hydrogen in oil, hydrogen sulfide and a small amount of light oil separates from tank top, through pipeline 19 carrying device, a small amount of light oil S20 is through the regular carrying device of pipeline 20. Remaining material S21 all returns tower top via pipeline 21 as backflow.
Be stripped of hydrogen, hydrogen sulfide refining boat coal S22 by extraction at the bottom of tower, first it is cooled to 175 DEG C through heat exchanger E4 with tower charging heat exchange, then it is cooled to 84 DEG C through heat exchanger E9 with the further heat exchange of raw material, finally it is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal. Heat at the bottom of fractionating column C1 tower is provided by reboiler furnace F2.
For guaranteeing boat product of coal quality, being provided with absorption digester R2 on boat product of coal line, described absorption digester R2 is connected with described water cooler E6.
Table 2 gives the thermic load data of each cold exchange device in this technique.
Table 2. is cold changes system heat load summary sheet (kW)
Embodiment 3
Furnace rear is adopted to include following operation (see accompanying drawing 3) when mixing hydrogen flow process
(1) reactive moieties
After boat coal raw material is pressurized, first after heat exchanger E1 with product heat exchange, enter raw materials furnace and heating F1 heating, then mix with recycle hydrogen, enter boat coal desulfurization alcohol reactor R1.
Hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously.
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after about 50 DEG C, entering cold high pressure separator D1.
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after high pressure hot separator oil gas heat exchange, enter the preheating of heating furnace convection section, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enter boat coal desulfurization alcohol reactor R1.
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1.
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats.
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower. Heat at the bottom of tower is provided by reboiler furnace F2. At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
For guaranteeing boat product of coal quality, boat product of coal line is provided with absorption digester R2.
Embodiment 4
Stokehold is adopted to include following operation (see accompanying drawing 4) when mixing hydrogen flow process
(1) reactive moieties
Boat coal raw material is pressurized and mixes with recycle hydrogen, first after heat exchanger E1 with product heat exchange, enters raw materials furnace and heating F1 heating, subsequently into boat coal desulfurization alcohol reactor R1.
Hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously.
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after about 50 DEG C, entering cold high pressure separator D1.
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after high pressure hot separator oil gas heat exchange, enter the preheating of heating furnace convection section, after then mixing with raw oil, enter heat exchanger E1 and product heat exchange.
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1.
(2) fractionating column part
Fractionating column part is identical with the mixed hydrogen flow process of furnace rear.
Comparative example 1
This comparative example is mixed hydrogen-cooled high division technique after adopting conventional oven, and technological process is referring to accompanying drawing 7.
(1) reactive moieties
Boat coal raw material S1 (40 DEG C after pressurized, 166 ton hour), first after heat exchanger E1 and product S5 heat exchange are to 241 DEG C, enter raw materials furnace and heating F1 heating to about 273.5 DEG C via pipeline 2, after mixing with recycle hydrogen S11 again, enter boat coal desulfurization alcohol reactor R1 via pipeline 4.
Boat coal desulfurization alcohol reactor R1 operating condition is 2.0MPa, 260 DEG C, and hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously.
Product S5 temperature 261 DEG C, bottom boat coal desulfurization alcohol reactor R1 out, first after heat exchanger E1 is cooled to 85.7 DEG C with raw material heat exchange, then through air cooler E2, water cooler E3 condensing cooling to after 50 DEG C, being entered cold high pressure separator D1 by pipeline 7, the vapour phase S8 rich in hydrogen flashed off in cold high pressure separator D1 enters surge tank D2 via pipeline 8.
Circulating hydrogen compressor K1 is entered after supplementing new hydrogen H2 rich in the oil gas S8 buffered tank D2 of hydrogen, through being sent to the preheating of heating furnace convection section by pipeline 10 after being pressurizeed by compressor, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil S3, enter boat coal desulfurization alcohol reactor R1 via pipeline 4.
By the product S12 (50 DEG C) separated bottom cold high pressure separator D1, through heat exchanger E4 be preheated to 220 DEG C from the refining boat coal S19 heat exchange bottom fractionating column C1 after, send into fractionating column C1.
(2) fractionating column part
Anti-afterproduct S13 after preheated enters the middle part of fractionating column C1, and it is 0.22MPa that fractionating column C1 operates pressure. In fractionating column C1, oil gas S14 rich in hydrogen, hydrogen sulfide is steamed by tower top, after air cooler E7, water cooler E8 condensing cooling are to about 40 DEG C, return tank D3 is entered through pipeline 15, the sour gas S16 being dissolved in the hydrogen in oil, hydrogen sulfide and a small amount of light oil separates from tank top, through pipeline 16 carrying device, a small amount of light oil S17 is through the regular carrying device of pipeline 17. Remaining material S18 all returns tower top via pipeline 18 as backflow.
Be stripped of hydrogen, hydrogen sulfide refining boat coal S19 by extraction at the bottom of tower, be first cooled to 82 DEG C through heat exchanger E4 with tower charging heat exchange, be cooled to less than 45 DEG C then through air cooler E5, water cooler E6, send battery limit (BL) as refining boat product of coal. Heat at the bottom of fractionating column C1 tower is provided by reboiler furnace F2.
For guaranteeing boat product of coal quality, boat product of coal line is provided with absorption digester R2.
Table 3 gives the thermic load data of each cold exchange device in this technique.
Table 3. is cold changes system heat load summary sheet (kW)
Comparative example 2
This comparative example is mixed hydrogen-cooled high division technique before adopting conventional oven, and technological process is referring to accompanying drawing 8.
It is different in that with comparative example 1: recycle hydrogen S11 mixes with boat coal raw material after heating furnace F1, but mixes with boat coal raw material S1 via pipeline 11 at heat exchanger E1 entrance. Mixed gas mixture S4 enters heat exchanger E1 and product S5 heat exchange via pipeline 4.
After mixed hydrogen, the heat exchange efficiency of heat exchanger E1 increases, and the material outlet temperature of heating furnace F1 is minimized (outlet temperature 260 DEG C).
Table 4 gives the thermic load data of each cold exchange device in this technique.
Table 4. is cold changes system heat load summary sheet (kW)
It can be seen that the energy resource consumption of the improvement technique of present invention proposition is significantly lower than conventional common process from above each example, and each technique adopts the energy resource consumption of the mixed hydrogen in stokehold want general and mix hydrogen technique lower than each corresponding furnace rear. Table 5 lists under various technique thermic load compare data.
The various process heat duty ratio of table 5 is relatively
In a word, contrast by above example Yu comparative example, after adopting the high pressure hot separator that the present invention proposes to add the high pressure hot separator kerosene hydrogenation technological process of cold high pressure separator, one side can make the cooling load reduction of response system more than 85%, high-temperature hot product makes fractionating column feeding temperature obtain certain raising on the other hand, thus causing that fractionating column reboiler heat duty reduces about 25%. And the vapour phase that high pressure hot separator flashes off and the heat exchange of recycle hydrogen or new hydrogen, then enable and measure with further recovery, directly reduce the thermic load about more than 5% of raw materials furnace and heating.
And raw material and the heat exchange of boat product of coal, reclaim the waste heat of boat product of coal on the one hand, on the other hand due to the raising of the coal raw material preheating temperature that navigates so that raw materials furnace and heating thermic load reduces about more than 30%.
After adopting the present invention, the public work of kerosene hydrogenation device cools down load reduction about 30%, and heating load reduces about 30%, and energy-saving effect is notable.
Claims (9)
1. the production technology of a kerosene hydrogenation, including reactive moieties and fractionating section, the product of described reactive moieties with boat coal raw material heat exchange after not cooled, it is directly entered high pressure hot separator, after air cooler is cooled to 45-55 DEG C, cold high pressure separator is entered after the vapour phase flashed off and recycle hydrogen or new hydrogen heat exchange, by the high-temperature reaction product separated bottom high pressure hot separator and cold high pressure separator with from after the refining boat coal heat exchange of Fractionator Bottom, feeding fractionating section.
2. the production technology of a kind of kerosene hydrogenation as claimed in claim 1, it is characterized in that, the product of described reactive moieties and boat coal raw material heat exchange, after the boat product of coal fractionated out from fractionating section and fractionating column charging heat exchange, as heat source medium and the boat further heat exchange of coal raw material.
3. the production technology of a kind of kerosene hydrogenation as claimed in claim 1 or 2, it is characterized in that, the production technology of described kerosene hydrogenation includes four kinds of technological processes: the mixed hydrogen of furnace rear adds raw produce heat exchange process, the mixed hydrogen in stokehold adds raw produce heat exchange process, the mixed hydrogen flow process of the mixed hydrogen flow process of furnace rear or stokehold.
4. the production technology of a kind of kerosene hydrogenation as claimed in claim 3, it is characterised in that described furnace rear mixed hydrogen includes following operation when adding raw produce heat exchange process:
(1) reactive moieties
After boat coal raw material pressurization, first boat product of coal heat exchange in heat exchanger E9 and from the hot side outlet of heat exchanger E4, after heat exchanger E1 and product heat exchange, enter raw materials furnace and heating F1 heating, after heating raw materials outlet of still mixes with recycle hydrogen, enter boat coal desulfurization alcohol reactor R1;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, it is sent in heat exchanger E3 by circulating hydrogen compressor pressurization and after the oil gas heat exchange of high pressure hot separator, enter the preheating of raw materials furnace and heating convection section, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enter boat coal desulfurization alcohol reactor R1;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower; Heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, then through heat exchanger E9 and the further heat exchange of raw material, is cooled to less than 45 DEG C through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal after.
5. the production technology of a kind of kerosene hydrogenation as claimed in claim 3, it is characterised in that the mixed hydrogen in described stokehold includes following operation when adding raw produce heat exchange process:
(1) reactive moieties
Boat coal raw material is pressurized and after mixing with recycle hydrogen, first boat product of coal heat exchange in heat exchanger E9 and from the hot side outlet of heat exchanger E4, after heat exchanger E1 and product heat exchange, enter raw materials furnace and heating F1 heating, subsequently into boat coal desulfurization alcohol reactor R1;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after then mixing with raw oil, enter heat exchanger E1 and product heat exchange;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, by obtaining refining boat coal at the bottom of tower; Heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, then through heat exchanger E9 and the further heat exchange of raw material, is cooled to less than 45 DEG C through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal after.
6. the production technology of a kind of kerosene hydrogenation as claimed in claim 3, it is characterised in that described furnace rear includes following operation when mixing hydrogen flow process:
(1) reactive moieties
After boat coal raw material is pressurized, first through in heat exchanger E1 with product heat exchange after, enter raw materials furnace and heating F1 heating, then mix with recycle hydrogen, enter the coal desulfurization alcohol reactor R1 that navigates;
In boat coal desulfurization alcohol reactor R1, hydrogenation reaction occurring, the non-hydrocarbons in fuel oil is removed effectively, and described non-hydrocarbons includes but not limited to sulfur, oxygen, nitrogen, and the some olefin in non-hydrocarbons, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after boat coal desulfurization alcohol reactor R1 entrance mixes with raw oil, enter boat coal desulfurization alcohol reactor R1;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, and by obtaining refining boat coal at the bottom of tower, heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
7. the production technology of a kind of kerosene hydrogenation as claimed in claim 3, it is characterised in that described stokehold includes following operation when mixing hydrogen flow process:
(1) reactive moieties
Boat coal raw material is pressurized and mix with recycle hydrogen, first through in heat exchanger E1 with product heat exchange after, enter raw materials furnace and heating F1 heating, subsequently into the coal desulfurization alcohol reactor R1 that navigates;
Hydrogenation reaction occurs in boat coal desulfurization alcohol reactor R1, and the non-hydrocarbons such as sulfur in fuel oil, oxygen, nitrogen is removed effectively, and some olefin, aromatic hydrocarbons are hydrogenated saturated simultaneously;
Product from boat coal desulfurization alcohol reactor R1 bottom out, first after heat exchanger E1 with raw material heat exchange, enter back into high pressure hot separator D4, the vapour phase rich in hydrogen flashed off in high pressure hot separator D4 is first through heat exchanger E3 and recycle hydrogen heat exchange, enter back into the further condensing cooling of air cooler E2 to after 45-55 DEG C, entering cold high pressure separator D1;
Oil-gas Separation in cold high pressure separator D1, tank deck enters circulating hydrogen compressor K1 after supplementing new hydrogen rich in the oil gas buffered tank D2 of hydrogen, pressurizeed by compressor and be sent to heat exchanger E3 and after the oil gas heat exchange of high pressure hot separator, enter the preheating of heating furnace convection section, after then mixing with raw oil, enter heat exchanger E1 and product heat exchange;
By the high-temperature reaction product separated bottom high pressure hot separator D4 and cold high pressure separator D1, through heat exchanger E4 with from after the refining boat coal heat exchange bottom fractionating column C1, sending into fractionating column C1;
(2) fractionating column part
The high-temperature hydrogenation oil discharged bottom cold high pressure separator D1, high pressure hot separator D4, enters fractionating column C1 after heat exchanger E4 preheats;
In fractionating column C1, the sour gas rich in hydrogen, hydrogen sulfide being dissolved in oil is separated by tower top, and by obtaining refining boat coal at the bottom of tower, heat at the bottom of tower is provided by reboiler furnace F2; At the bottom of tower, refining boat coal is first through heat exchanger E4 and tower charging heat exchange, is cooled to less than 45 DEG C then through air cooler E5, water cooler E6, sends battery limit (BL) as refining boat product of coal.
8. the production technology of a kind of kerosene hydrogenation as described in one of claim 4 to 7, it is characterised in that being provided with absorption digester R2 on boat product of coal line, described absorption digester R2 is connected with described water cooler E6.
9. a production system for kerosene hydrogenation, it includes the production technology of kerosene hydrogenation described for one of claim 1-8.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108795490A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | It reforms full fraction and generates oily hydrogenation plant and cut light tower coupled system |
| CN108795494A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | Recapitalization generating oil hydrogenation device and cut light tower coupled system |
| CN113698955A (en) * | 2020-05-21 | 2021-11-26 | 中国石油天然气集团有限公司 | Aviation kerosene hydrogenation reaction product treatment system |
| CN116410770A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Aviation kerosene hydrogenation system adopting nitrogen stripping |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289631A (en) * | 2008-03-12 | 2008-10-22 | 上海九元石油化工有限公司 | Optimizing hydrogenation and heat-exchange system |
| CN204058379U (en) * | 2014-06-06 | 2014-12-31 | 上海华西化工科技有限公司 | A kind of catalytic diesel oil hydro-upgrading unit heat exchange optimization system inferior |
| CN104611019A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy consumption hydrocracking method for producing high-quality jet fuel |
-
2016
- 2016-02-01 CN CN201610069300.4A patent/CN105670689A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101289631A (en) * | 2008-03-12 | 2008-10-22 | 上海九元石油化工有限公司 | Optimizing hydrogenation and heat-exchange system |
| CN104611019A (en) * | 2013-11-05 | 2015-05-13 | 中国石油化工股份有限公司 | Low energy consumption hydrocracking method for producing high-quality jet fuel |
| CN204058379U (en) * | 2014-06-06 | 2014-12-31 | 上海华西化工科技有限公司 | A kind of catalytic diesel oil hydro-upgrading unit heat exchange optimization system inferior |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108795490A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | It reforms full fraction and generates oily hydrogenation plant and cut light tower coupled system |
| CN108795494A (en) * | 2017-05-04 | 2018-11-13 | 中国石油化工股份有限公司 | Recapitalization generating oil hydrogenation device and cut light tower coupled system |
| CN108795494B (en) * | 2017-05-04 | 2023-07-28 | 中国石油化工股份有限公司 | Coupling system of hydrogenation device and light component removing tower for reforming generated oil |
| CN108795490B (en) * | 2017-05-04 | 2023-07-28 | 中国石油化工股份有限公司 | Coupling system of hydrogenation device and light component removal tower for reforming full distillate generated oil |
| CN113698955A (en) * | 2020-05-21 | 2021-11-26 | 中国石油天然气集团有限公司 | Aviation kerosene hydrogenation reaction product treatment system |
| CN116410770A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Aviation kerosene hydrogenation system adopting nitrogen stripping |
| CN116410770B (en) * | 2021-12-31 | 2024-04-30 | 中国石油天然气股份有限公司 | Aviation kerosene hydrogenation system adopting nitrogen stripping |
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