CN103421540A - Oil-gas separation process of catalytic reforming device - Google Patents
Oil-gas separation process of catalytic reforming device Download PDFInfo
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- CN103421540A CN103421540A CN2013103451770A CN201310345177A CN103421540A CN 103421540 A CN103421540 A CN 103421540A CN 2013103451770 A CN2013103451770 A CN 2013103451770A CN 201310345177 A CN201310345177 A CN 201310345177A CN 103421540 A CN103421540 A CN 103421540A
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Abstract
The invention discloses an oil-gas separation process of a catalytic reforming device, and the oil-gas separation process is proposed based on energy transfer and low-temperature residual heat upcycling as well as a working principle of a compressor. According to the oil-gas separation process, a cooling load of an oil-gas separation subsystem is successfully transferred to a downstream product separation subsystem by arranging a first separation tank an outlet of a first heat exchanger, and the handling capacity of the compressor is successfully reduced and meanwhile the purity of circulating hydrogen and product hydrogen is improved by reducing the intake air temperature of the circulating hydrogen compressor. According to the oil-gas separation process, the flow path and the control scheme of the device are not changed and both the quality and the yield of a liquid-phase oil product cannot be influenced.
Description
Technical field
The present invention relates to the technical field of catalytic reforming unit, refer in particular to a kind of gas-oil separation technique of catalytic reforming unit.
Background technology
Catalytic reforming is to produce the important means of low-carbon (LC) aromatic hydrocarbons and clean gasoline with high octane in oil refining process, is also the important hydrogen source of oil refining enterprise simultaneously, and it is comprised of raw materials pretreatment, reforming reaction, gas-oil separation and product separation four parts.Wherein gas-oil separation is partly being born the task of the reforming reaction product separation being become to hydrogen-rich gas and reformate, its basic procedure is (as shown in Figure 2): from the reaction product of reforming reactor first through E0201 with reformer feed from the refining petroleum naphtha 01 of pretreatment system and the mixture heat exchange of recycle hydrogen, then advance air cooler A0201 condensing cooling, then advance separating tank D0202 and isolate hydrogen-rich gas and reformate.Wherein, hydrogen-rich gas advances circulating hydrogen compressor K0201, after pressure-raising, one tunnel is returned to the reforming reaction system and is participated in reaction, supercharger (K0202/1 and K0202/2) is advanced on another road, through mixing after pressure-raising with from separating tank D0202 the reformate after pump P0201AB pressure-raising, through the laggard contact tank again of water recirculator E0203 D0205, implement to contact again, at low temperature, further adsorb hydro carbons wherein by reformate under condition of high voltage, obtain (approximately 92%) hydrogen that purity is higher, advance again hydrogen pipe network 02 after directly advancing hydrogen pipe network 02 or sending the PSA/ film separation unit further to purify, after mixing, certainly compresses into the isolated reformate of separating tank D0203 and D0204 the depentanizer 03 of the product separation part in downstream.
In above-mentioned flow process, the reforming reaction product from E0201 temperature out usually more than 100 ℃, directly advance air cooler A0201, not only strengthened cooling load, also reduced the temperature that reformate advances depentanizer 03, can improve the thermal load of reboiler furnace at the bottom of its tower.In addition, because the service temperature of separating tank D0202 is higher, make the inlet temperature of circulating hydrogen compressor K0201 higher, recycle hydrogen concentration is low, treatment capacity strengthens, and finally causes driving the steam consumption quantity of turbine to increase.Therefore, the heat of reforming reaction product secondary is transferred to the downstream fractionating system from air cooler A0201, and cooling operation separating tank D0202, for the energy consumption that reduces oil and gas separating system and depentanizer, be vital, the present invention just is being based on these 2 considerations and is putting forward.
Summary of the invention
The object of the invention is to overcome in the gas-oil separation technique of existing catalytic reforming unit, the heat of reforming reaction product secondary does not reclaim, and the separating tank service temperature is higher, cause cooling load large, the circulating hydrogen compressor inlet temperature is high, recycle hydrogen concentration is low, treatment capacity is large, reformate advances the shortcoming that the depentanizer temperature is low, provides a kind of reforming reaction product secondary heat that shifts to derived product separation system and the gas-oil separation technique that realizes the catalytic reforming unit of flash liberation tank lower temperature operation.
For achieving the above object, technical scheme provided by the present invention is: a kind of gas-oil separation technique of catalytic reforming unit comprises the following steps:
1) from the reaction product of reforming reactor through First Heat Exchanger refining petroleum naphtha and laggard the first separating tank of recycle hydrogen mixture heat exchange with reforming reaction system from upstream, separate gas and reformate;
2) gas that the first separating tank separates is cooled to 10 ℃ of-20 ℃ of laggard second separating tanks through the first air cooler and the first water cooler successively, separates hydrogen-rich gas and liquid phase oil product, and now, this second separating tank is in 10 ℃ of-20 ℃ of operations;
3) hydrogen-rich gas that the second separating tank separates advances circulating hydrogen compressor, be divided into two-way after this circulating hydrogen compressor pressure-raising, wherein the reforming reaction system of upstream is returned on a road, and another Lu Zejing second air cooler is cooled to 38 ℃ of-55 ℃ of laggard the 3rd separating tanks, separates gas phase and reformate;
4) gas phase that the 3rd separating tank separates is advanced after the first supercharger pressure-raising with the liquid phase oil product of contact tank again from downstream to mix, and mixes and is cooled to 38 ℃ of-55 ℃ of laggard the 4th separating tanks by the 3rd air cooler, separates gas and reformate;
5) gas that the 4th separating tank separates is after the second supercharger pressure-raising, advance successively after the 4th air cooler and the second water cooler are cooled to 25 ℃-40 ℃ and mix with the liquid phase oil product from the second separating tank, mix laggard contact tank again, separate hydrogen, now, this again contact tank in 15 ℃ of-25 ℃ of operations;
6) hydrogen that contact tank separates again is final to be sent to toward the hydrogen pipe network, and after coming from the reformate mixing of the 3rd separating tank and the 4th separating tank, from compressing into the second interchanger, and after being heated to 60 ℃-85 ℃ with the tower top oil gas of the depentanizer in downstream, with the reformate from the first separating tank, mix, after mixing from the depentanizer in force feed downstream.
The gas that the liquid phase oil product of described the second separating tank just separates with the 4th separating tank after the pump pressure-raising mixes.
The hydrogen that described contact tank again separates advances the hydrogen pipe network after the PSA/ film separation unit is purified again.
Described the first water cooler is 7 ℃ of cold water water coolers, and its cold water is provided by the lithiumbromide Hot water units.
Described the second water cooler is water recirculator.
The present invention compared with prior art, has following advantage and beneficial effect:
1, in First Heat Exchanger outlet, the first separating tank is set, and keeps gas phase to walk former flow process advancing the first air cooler, liquid phase self-pressure is directly removed depentanizer, and this has reduced the cooling load 9.5 * 10 of reforming reaction product secondary
4Kw-4.3 * 10
3Kw;
2, the import at the second separating tank arranges the first water cooler, cold water originates from absorption lithiumbromide water-heating cooling unit, hot water is occurred by the device low temperature exhaust heat, 12 ℃-22 ℃ of the temperature that this has reduced the reformate separating tank, the treatment capacity 5422Nm that is conducive to improve recycle hydrogen concentration 2.5%-1.9% and reduces circulating hydrogen compressor
3/ h-5692Nm
312 ℃-22 ℃ of/h and inlet air temperature, thus circulating hydrogen compressor energy consumption 529kw-570kw reduced;
3, be provided with the second interchanger, with the tower top oil gas preheating depentanizer charging of depentanizer, improved 11.1 ℃-15.1 ℃ of the temperature that reformate advances depentanizer, be conducive to reduce at the bottom of its tower boiling hot load 1.5 * 10 again
3Kw-3.0 * 10
3Kw;
4,, due to the needs water-heating cooling, increased refinery's Low Temperature Thermal trap load 7.88 * 10
3-8.25 * 10
3Kw, be conducive to the operation of steady two season of summer in winter hot-water system.
The accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
The process flow diagram that Fig. 2 is prior art.
Embodiment
Below in conjunction with a plurality of specific embodiments, the invention will be further described.
Shown in Figure 1, the gas-oil separation technique of the described catalytic reforming unit of the present embodiment, concrete situation is as follows: from the reaction product (527 ℃, 0.316MPag, 273.9t/h) of reforming reactor through First Heat Exchanger E201 refining petroleum naphtha 1(89 ℃, 1.0MPag, 242t/h with reforming reaction system from upstream) and recycle hydrogen (81.7 ℃, 0.51Mpag, moles of hydrogen concentration 91.8%, 31.8t/h) mixture heat exchange after 104 ℃ advance the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 ℃) and reformate (76.5t/h, 102 ℃, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 ℃) (load of corresponding the first air cooler A201 is 1.99 * 10 to be cooled to 50 ℃ through the first air cooler A201
4Kw), and then advance this first water cooler of the first water cooler EN1(EN1 and be specially 7 ℃ of cold water water coolers, its cold water is provided by the lithiumbromide Hot water units, hot water is produced by the low temperature exhaust heat of catalytic reforming unit), the load that is further cooled to 18 ℃ of corresponding first water cooler EN1 of laggard the second separating tank D202(is 5.0 * 10
3Kw in addition, in order to reduce the low temperature cold water consumption of the first water cooler EN1, also can arrange and a water recirculator charging of the first water cooler EN1 is cooled to approximately 32 ℃ before the first water cooler EN1).Now, this second separating tank D202, in 18 ℃ of lower temperature operation, separates hydrogen-rich gas 235360Nm
3/ h(0.24Mpag, moles of hydrogen concentration 91.8%) and the liquid phase oil product, and the hydrogen-rich gas 235360Nm that this second separating tank D202 separates
3/ h(0.24Mpag, moles of hydrogen concentration 91.8%) send circulating hydrogen compressor K201 to boost to 0.51Mpag(81.7 ℃) after be divided into two-way, a road 125712Nm wherein
3/ h returns to the reforming reaction system response of upstream, another road 109648Nm
3/ h advances the second air cooler A202 and is cooled to 50 ℃ (load of corresponding the second air cooler A202 is 1.7 * 10
3kw), then advance the 3rd separating tank D203, further separate gas phase 109648Nm
3/ h and reformate (0t/h, 50 ℃), and the gas phase 109648Nm that the 3rd separating tank D203 separates
3/ h advances the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 ℃) after, mix 61 ℃ with the liquid phase oil product (20 ℃, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and advance the 3rd air cooler A203 and be cooled to 50 ℃ (load of corresponding the 3rd air cooler A203 is 2.6 * 10
3kw) laggard the 4th separating tank D204, separate gas 110822Nm
3/ h and reformate (145.8t/h, 50 ℃), and the gas 110822Nm that the 4th separating tank D204 separates
3/ h advances the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 ℃) laggard the 4th air cooler A204 is cooled to 50 ℃ (load of corresponding the 4th air cooler A204 is 3.9 * 10
3kw) after, then advance this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding the second water cooler E203 is 4.0 * 10 to be cooled to 32 ℃
2kw) after, after from the second separating tank D202 the liquid phase oil product after pump P201AB pressure-raising (18 ℃, 137.7t/h, 2.7MPa), being mixed into 25 ℃, then advance contact tank D205 again, the hydrogen 106880Nm that to separate volumetric molar concentration be 94%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 ℃) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 after the PSA/ film separation unit is purified again, and come from the reformate (0t/h of the 3rd separating tank D203, 50 ℃) and the reformate (145.8t/h of the 4th separating tank D204, 50 ℃), mix rear 50 ℃ (145.8t/h) and certainly compress into the second interchanger EN2, with (104.6 ℃ of the tower top oil gas of the depentanizer 3 in downstream, 43.3t/h, 1.0MPa) (load of corresponding the second interchanger EN2 is 2.0 * 10 to be heated 70 ℃
3and to mix rear 80 ℃ (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of the depentanizer 3(in force feed downstream with reformate (76.5t/h, 102 ℃, 0.3MPa) from the first separating tank DN1 be 1.05 * 10 kw),
4kw).
The gas-oil separation technique of the described catalytic reforming unit of the present embodiment as different from Example 1, concrete situation is as follows: from the reaction product (527 ℃, 0.316MPag, 273.9t/h) of reforming reactor through First Heat Exchanger E201 refining petroleum naphtha 1(89 ℃, 1.0MPag, 242t/h with reforming reaction system from upstream) and recycle hydrogen (81.7 ℃, 0.51Mpag, moles of hydrogen concentration 92.2%, 31.8t/h) mixture heat exchange after 104 ℃ advance the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 ℃) and reformate (76.5t/h, 102 ℃, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 ℃) (load of corresponding the first air cooler A201 is 1.99 * 10 to be cooled to 50 ℃ through the first air cooler A201
4Kw), and then advance this first water cooler of the first water cooler EN1(EN1 and be specially 7 ℃ of cold water water coolers, its cold water is provided by the lithiumbromide Hot water units, hot water is produced by the low temperature exhaust heat of catalytic reforming unit), the load that is further cooled to 10 ℃ of corresponding first water cooler EN1 of laggard the second separating tank D202(is 6.25 * 10
3Kw in addition, in order to reduce the low temperature cold water consumption of the first water cooler EN1, also can arrange and a water recirculator charging of the first water cooler EN1 is cooled to approximately 32 ℃ before the first water cooler EN1).Now, this second separating tank D202, in 10 ℃ of lower temperature operation, separates hydrogen-rich gas 235110Nm
3/ h(0.24Mpag, moles of hydrogen concentration 92.2%) and the liquid phase oil product, and the hydrogen-rich gas 235110Nm that this second separating tank D202 separates
3/ h(0.24Mpag, moles of hydrogen concentration 92.2%) send circulating hydrogen compressor K201 to boost to 0.51Mpag(78 ℃) after be divided into two-way, a road 125712Nm wherein
3/ h returns to the reforming reaction system response of upstream, another road 125462Nm
3/ h advances the second air cooler A202 and is cooled to 38 ℃ (load of corresponding the second air cooler A202 is 2 * 10
3kw), then advance the 3rd separating tank D203, further separate gas phase 109611Nm
3/ h and reformate (0t/h, 38 ℃), and the gas phase 109611Nm that the 3rd separating tank D203 separates
3/ h advances the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 ℃) after, mix 55 ℃ with the liquid phase oil product (15 ℃, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and advance the 3rd air cooler A203 and be cooled to 38 ℃ (load of corresponding the 3rd air cooler A203 is 3 * 10
3kw) laggard the 4th separating tank D204, separate gas 110600Nm
3/ h and reformate (145.8t/h, 38 ℃), and the gas 110600Nm that the 4th separating tank D204 separates
3/ h advances the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 ℃) laggard the 4th air cooler A204 is cooled to 38 ℃ (load of corresponding the 4th air cooler A204 is 4.5 * 10
3kw) after, then advance this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding the second water cooler E203 is 2.0 * 10 to be cooled to 32 ℃
2kw) after, after from the second separating tank D202 the liquid phase oil product after pump P201AB pressure-raising (10 ℃, 137.7t/h, 2.7MPa), being mixed into 15 ℃, then advance contact tank D205 again, the hydrogen 106770Nm that to separate volumetric molar concentration be 94.2%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 ℃) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 after the PSA/ film separation unit is purified again, and come from the reformate (0t/h of the 3rd separating tank D203, 38 ℃) and the reformate (145.8t/h of the 4th separating tank D204, 38 ℃), mix rear 38 ℃ (145.8t/h) and certainly compress into the second interchanger EN2, with (104.6 ℃ of the tower top oil gas of the depentanizer 3 in downstream, 43.3t/h, 1.0MPa) (load of corresponding the second interchanger EN2 is 2.1 * 10 to be heated 60 ℃
3and to mix rear 75 ℃ (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of the depentanizer 3(in force feed downstream with reformate (76.5t/h, 102 ℃, 0.3MPa) from the first separating tank DN1 be 1.08 * 10 kw),
4kw).
Embodiment 3
The gas-oil separation technique of the described catalytic reforming unit of the present embodiment as different from Example 1, concrete situation is as follows: from the reaction product (527 ℃, 0.316MPag, 273.9t/h) of reforming reactor through First Heat Exchanger E201 refining petroleum naphtha 1(89 ℃, 1.0MPag, 242t/h with reforming reaction system from upstream) and recycle hydrogen (81.7 ℃, 0.51Mpag, moles of hydrogen concentration 91.6%, 31.8t/h) mixture heat exchange after 104 ℃ advance the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 ℃) and reformate (76.5t/h, 102 ℃, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 ℃) (load of corresponding the first air cooler A201 is 1.99 * 10 to be cooled to 50 ℃ through the first air cooler A201
4Kw), and then advance this first water cooler of the first water cooler EN1(EN1 and be specially 7 ℃ of cold water water coolers, its cold water is provided by the lithiumbromide Hot water units, hot water is produced by the low temperature exhaust heat of catalytic reforming unit), the load that is further cooled to 20 ℃ of corresponding first water cooler EN1 of laggard the second separating tank D202(is 4.8 * 10
3Kw in addition, in order to reduce the low temperature cold water consumption of the first water cooler EN1, also can arrange and a water recirculator charging of the first water cooler EN1 is cooled to approximately 32 ℃ before the first water cooler EN1).Now, this second separating tank D202, in 20 ℃ of lower temperature operation, separates hydrogen-rich gas 235380Nm
3/ h(0.24Mpag, moles of hydrogen concentration 91.6%) and the liquid phase oil product, and the hydrogen-rich gas 235380Nm that this second separating tank D202 separates
3/ h(0.24Mpag, moles of hydrogen concentration 91.6%) send circulating hydrogen compressor K201 to boost to 0.51Mpag(81.7 ℃) after be divided into two-way, a road 125712Nm wherein
3/ h returns to the reforming reaction system response of upstream, another road 109668Nm
3/ h advances the second air cooler A202 and is cooled to 55 ℃ (load of corresponding the second air cooler A202 is 1.2 * 10
3kw), then advance the 3rd separating tank D203, further separate gas phase 109648Nm
3/ h and reformate (0t/h, 55 ℃), and the gas phase 109648Nm that the 3rd separating tank D203 separates
3/ h advances the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 ℃) after, mix 61 ℃ with the liquid phase oil product (25 ℃, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and advance the 3rd air cooler A203 and be cooled to 55 ℃ (load of corresponding the 3rd air cooler A203 is 2.0 * 10
3kw) laggard the 4th separating tank D204, separate gas 110822Nm
3/ h and reformate (145.8t/h, 55 ℃), and the gas 110822Nm that the 4th separating tank D204 separates
3/ h advances the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 ℃) laggard the 4th air cooler A204 is cooled to 55 ℃ (load of corresponding the 4th air cooler A204 is 3.5 * 10
3kw) after, then advance this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding the second water cooler E203 is 4.3 * 10 to be cooled to 32 ℃
2kw) after, after from the second separating tank D202 the liquid phase oil product after pump P201AB pressure-raising (20 ℃, 137.7t/h, 2.7MPa), being mixed into 25 ℃, then advance contact tank D205 again, the hydrogen 106890Nm that to separate volumetric molar concentration be 93.8%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 ℃) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 after the PSA/ film separation unit is purified again, and come from the reformate (0t/h of the 3rd separating tank D203, 55 ℃) and the reformate (145.8t/h of the 4th separating tank D204, 50 ℃), mix rear 55 ℃ (145.8t/h) and certainly compress into the second interchanger EN2, with (104.6 ℃ of the tower top oil gas of the depentanizer 3 in downstream, 43.3t/h, 1.0MPa) (load of corresponding the second interchanger EN2 is 2.9 * 10 to be heated 85 ℃
3and to mix rear 90 ℃ (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of the depentanizer 3(in force feed downstream with reformate (76.5t/h, 102 ℃, 0.3MPa) from the first separating tank DN1 be 9.0 * 10 kw),
3kw).
Shown in Figure 2, from the reaction product (527 ℃, 0.316MPag, 281.3t/h) of reforming reactor through interchanger E0201 refining petroleum naphtha 01(89 ℃, 1.0MPag, 242t/h with reforming reaction system from upstream) and recycle hydrogen (101.4 ℃, 0.51Mpag, moles of hydrogen concentration 89.7%, 39.3t/h) mixture heat exchange after 104 ℃ advance air cooler A0201, being cooled to 50 ℃ of loads that advance the corresponding air cooler A0201 of separating tank D0202(is 2.62 * 10
4Kw), separate hydrogen-rich gas 240802Nm
3/ h(0.24Mpag, moles of hydrogen concentration 89.7%) and the liquid phase oil product, now, the service temperature of this second separating tank D0202 is 50 ℃, and the hydrogen-rich gas 240802Nm that this separating tank D0202 separates
3/ h(0.24Mpag, moles of hydrogen concentration 89.7%) send circulating hydrogen compressor K0201 to boost to 0.51Mpag(101.4 ℃) after be divided into two-way, a road 128610Nm wherein
3/ h returns to the reforming reaction system response of upstream, another road 112192Nm
3/ h advances air cooler A0202 and is cooled to 50 ℃ (load of corresponding air cooler A0202 is 2.8 * 10
3Kw), then advance separating tank D0203 and further separate gas phase 112098Nm
3/ h and reformate (3.2t/h, 50 ℃), and the gas phase 112098Nm that this separating tank D0203 separates
3/ h send the first supercharger K0202/1, pressure-raising is to 1.36Mpag(135 ℃) after, mix 65 ℃ with the liquid phase oil product (32 ℃, 2.51Mpag, 213.3t/h) of the D0205 of contact tank again from downstream and advance air cooler A0203 and be cooled to 50 ℃ (load of corresponding air cooler A0203 is 4.0 * 10
3Kw) laggard separating tank D0204, separate gas 110948Nm
3/ h and reformate (218.9t/h, 50 ℃), and the gas 110948Nm that this separating tank D0204 separates
3/ h advances the second supercharger K0202/2, by pressure-raising to 2.59Mpag(118 ℃) laggard air cooler A0204 is cooled to 50 ℃ (load of corresponding air cooler A0204 is 3.8 * 10
3Kw) after, with mix 50 ℃ of this water cooler of water inlet cooler E0203(E0203 from separating tank D0202 the liquid phase oil product after pump P0201AB pressure-raising (50 ℃, 203.4t/h, 0.24MPa) and be specially water recirculator) be cooled to 32 ℃ after, then the load that advances again the corresponding water cooler E0203 of contact tank D0205(is 1.4 * 10
3Kw), separate the hydrogen 106942Nm that volumetric molar concentration is 93.9%
3/ h(2.51Mpag), this hydrogen that contact tank D0205 separates again finally send hydrogen pipe network 02 after the PSA/ film separation unit is purified again, and come from the reformate (3.2t/h, 50 ℃) of separating tank D0203 and the reformate of separating tank D0204 (218.9t/h, 50 ℃), mixing rear 50 ℃ (222.1t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of the depentanizer 03(in force feed downstream is 1.2 * 10
4Kw).
In sum, gas-oil separation technique compared to existing technology, the first separating tank DN1 and the first water cooler EN1 and the about 290m of the second interchanger EN2(total area have been set up in flowage structure of the present invention aspect
2); And of the present invention with can aspect in conjunction with above-mentioned three specific embodiments, situation is as follows:
Embodiment 1:
1), the cooling load of the first air cooler A201 is by 2.62 * 10
4Kw is reduced to 1.99 * 10
4Kw, reduce 6.3 * 10
3Kw; The cooling load of the second air cooler A202 is by 2.8 * 10
3Kw is reduced to 1.7 * 10
3Kw, reduce 1.1 * 10
3Kw; The cooling load of the 3rd air cooler A203 is by 4.0 * 10
3Kw is reduced to 2.6 * 10
3Kw, reduce 1.4 * 10
3Kw; The cooling load of the 4th air cooler A204 is by 3.8 * 10
3Kw is elevated to 3.9 * 10
3Kw, increase by 1.0 * 10
2Kw; The cooling load of the second water cooler E203 is by 1.4 * 10
3Kw is reduced to 4.0 * 10
2Kw, reduce 1.0 * 10
3Kw; The cooling load of the tower top oil gas of depentanizer 3 is by 5.12 * 10
3Kw is reduced to 3.03 * 10
3Kw, reduce 2.09 * 10
3Kw; The cooling load of the first water cooler EN1 is 7.45 * 10
3Kw.Add up to total cooling load by 4.33 * 10 before changing
4Kw is reduced to 3.89 * 10
4Kw, reduce 4.34 * 10
3Kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235360Nm
3/ h, reduce 5442Nm
3/ h, corresponding effective power consumption is reduced to 6392kw by 6932kw, reduces 540kw; Simultaneously, the effective power consumption of the first supercharger K202/1 is reduced to 4460kw by 4499kw, reduces 39kw; The effective power consumption of the second supercharger K202/2 is reduced to 3433kw by 3439kw, reduces 6kw; Add up to the total effective power consumption of compressor to be reduced to 14285kw by the 14870kw before changing, reduce 585kw.
3), the volumetric molar concentration of recycle hydrogen brings up to 91.8% by 89.7% before changing, and increases by 2.1%; The volumetric molar concentration of product hydrogen brings up to 94% by 93.9% before changing, and increases by 0.1%.
4), the feeding temperature of depentanizer 3 is elevated to 197.7 ℃ by 186.6 ℃ before changing, and improves 11.1 ℃, so at the bottom of tower the furnace capacity of reboiler furnace from 1.2 * 10
4Kw is reduced to 1.05 * 10
4Kw, reduce 1.5 * 10
3Kw.
5), the dissolved hydrogen that advances depentanizer 3 with reformate drops to 24.9kg/h by the 32.1kg/h before changing, and reduces 7.2kg/h.
Therefore, comprehensively above-mentioned, in embodiment 1, compared to existing technology, its total cooling load descends 4.34 * 10 in the present invention
3Kw, total process furnace furnace capacity descends 1.7 * 10
3Kw, total compressor effective power consumption decline 585kw, total hydrogen loss reduces 7.2kg/h.Get 90% by 4000 yuan/t(of standard fuel oil heater efficiency), 0.3 yuan/t(of the recirculated water recirculated water temperature difference gets 8 ℃), 0.6 yuan/kwh(of electricity price Compressor Group total efficiency gets 65%), 20000 yuan/t of hydrogen valency calculates, overall running cost reduces by 1466.9 yuan/h, rolls over 1,232 ten thousand yuan/year (device is got 8400 hours a year working time).
Embodiment 2:
1), the cooling load of the first air cooler A201 is by 2.62 * 10
4Kw is reduced to 1.99 * 10
4Kw, reduce 6.3 * 10
3Kw; The cooling load of the second air cooler A202 is by 2.8 * 10
3Kw is reduced to 2.0 * 10
3Kw, reduce 8.0 * 10
2Kw; The cooling load of the 3rd air cooler A203 is by 4.0 * 10
3Kw is reduced to 3.0 * 10
3Kw, reduce 1.0 * 10
3Kw; The cooling load of the 4th air cooler A204 is by 3.8 * 10
3Kw is elevated to 4.5 * 10
3Kw, increase by 7.0 * 10
2Kw; The cooling load of the second water cooler E203 is by 1.4 * 10
3Kw is reduced to 2.0 * 10
2Kw, reduce 1.2 * 10
3Kw; The cooling load of the tower top oil gas of depentanizer 3 is by 5.12 * 10
3Kw is reduced to 3.0 * 10
3Kw, reduce 2.1 * 10
3Kw; The cooling load of the first water cooler EN1 is 8.25 * 10
3Kw.Add up to total cooling load by 4.33 * 10 before changing
4Kw is reduced to 3.38 * 10
4Kw, reduce 9.5 * 10
4Kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235110Nm
3/ h, reduce 5692Nm
3/ h, corresponding effective power consumption is reduced to 6362kw by 6932kw, reduces 570kw; Simultaneously, the effective power consumption of the first supercharger K202/1 is reduced to 4450kw by 4499kw, reduces 49kw; The effective power consumption of the second supercharger K202/2 is reduced to 3433kw by 3439kw, reduces 6kw; Add up to the total effective power consumption of compressor to be reduced to 14245kw by the 14870kw before changing, reduce 625kw.
3), the volumetric molar concentration of recycle hydrogen brings up to 92.2% by 89.7% before changing, and increases by 2.5%; The volumetric molar concentration of product hydrogen brings up to 94.2% by 93.9% before changing, and increases by 0.3%.
4), the feeding temperature of depentanizer 3 is elevated to 197.7 ℃ by 186.6 ℃ before changing, and improves 11.1 ℃, so at the bottom of tower the furnace capacity of reboiler furnace from 1.2 * 10
4Kw is reduced to 1.05 * 10
4Kw, reduce 1.5 * 10
3Kw.
5), the dissolved hydrogen that advances depentanizer 3 with reformate drops to 24.5kg/h by the 32.1kg/h before changing, and reduces 7.4kg/h.
Therefore, comprehensively above-mentioned, in embodiment 2, compared to existing technology, its total cooling load descends 9.5 * 10 in the present invention
3Kw, total process furnace furnace capacity descends 1.5 * 10
3Kw, total compressor effective power consumption decline 625kw, total hydrogen loss reduces 7.4kg/h.Get 90% by 4000 yuan/t(of standard fuel oil heater efficiency), 0.3 yuan/t(of the recirculated water recirculated water temperature difference gets 8 ℃), 0.6 yuan/kwh(of electricity price Compressor Group total efficiency gets 65%), 20000 yuan/t of hydrogen valency calculates, overall running cost reduces by 1580.9 yuan/h, rolls over 1,328 ten thousand yuan/year (device is got 8400 hours a year working time).
Embodiment 3:
1), the cooling load of the first air cooler A201 is by 2.62 * 10
4Kw is reduced to 1.99 * 10
4Kw, reduce 6.3 * 10
3Kw; The cooling load of the second air cooler A202 is by 2.8 * 10
3Kw is reduced to 1.7 * 10
3Kw, reduce 1.1 * 10
3Kw; The cooling load of the 3rd air cooler A203 is by 4.0 * 10
3Kw is reduced to 2.6 * 10
3Kw, reduce 1.4 * 10
3Kw; The cooling load of the 4th air cooler A204 is by 3.8 * 10
3Kw is elevated to 3.9 * 10
3Kw, increase by 1.0 * 10
2Kw; The cooling load of the second water cooler E203 is by 1.4 * 10
3Kw is reduced to 4.0 * 10
2Kw, reduce 1.0 * 10
3Kw; The cooling load of the tower top oil gas of depentanizer 3 is by 5.12 * 10
3Kw is reduced to 3.03 * 10
3Kw, reduce 2.09 * 10
3Kw; The cooling load of the first water cooler EN1 is 7.88 * 10
3Kw.Add up to total cooling load by 4.33 * 10 before changing
4Kw is reduced to 3.9 * 10
4Kw, reduce 4.3 * 10
3Kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235380Nm
3/ h, reduce 5422Nm
3/ h, corresponding effective power consumption is reduced to 6502kw by 6932kw, reduces 529kw; Simultaneously, the effective power consumption of the first supercharger K202/1 is reduced to 4465kw by 4499kw, reduces 34kw; The effective power consumption of the second supercharger K202/2 is reduced to 3433kw by 3439kw, reduces 6kw; Add up to the total effective power consumption of compressor to be reduced to 14307kw by the 14870kw before changing, reduce 563kw.
3), the volumetric molar concentration of recycle hydrogen brings up to 91.6% by 89.7% before changing, and increases by 1.9%; The volumetric molar concentration of product hydrogen is reduced to 93.8% by 93.9% before changing, and reduces 0.1%.
4), the feeding temperature of depentanizer 3 is elevated to 198.7 ℃ by 186.6 ℃ before changing, and improves 12.1 ℃, so at the bottom of tower the furnace capacity of reboiler furnace from 1.2 * 10
4Kw is reduced to 9.0 * 10
3Kw, reduce 3.0 * 10
3Kw.
5), the dissolved hydrogen that advances depentanizer 3 with reformate drops to 26.9kg/h by the 32.1kg/h before changing, and reduces 5.2kg/h.
Therefore, comprehensively above-mentioned, in embodiment 3, compared to existing technology, its total cooling load descends 4.3 * 10 in the present invention
3Kw, total process furnace furnace capacity descends 3.0 * 10
3Kw, total compressor effective power consumption decline 563kw, total hydrogen loss reduces 5.2kg/h.Get 90% by 4000 yuan/t(of standard fuel oil heater efficiency), 0.3 yuan/t(of the recirculated water recirculated water temperature difference gets 8 ℃), 0.6 yuan/kwh(of electricity price Compressor Group total efficiency gets 65%), 20000 yuan/t of hydrogen valency calculates, overall running cost reduces by 1211.9 yuan/h, rolls over 1,017 ten thousand yuan/year (device is got 8400 hours a year working time).
The examples of implementation of the above are only the present invention's preferred embodiment, not with this, limit practical range of the present invention, therefore the variation that all shapes according to the present invention, principle are done all should be encompassed in protection scope of the present invention.
Claims (5)
1. the gas-oil separation technique of a catalytic reforming unit, is characterized in that, comprises the following steps:
1) from the reaction product of reforming reactor through First Heat Exchanger (E201) refining petroleum naphtha (1) and laggard the first separating tank of recycle hydrogen mixture heat exchange (DN1) with reforming reaction system from upstream, separate gas and reformate;
2) gas that the first separating tank (DN1) separates is cooled to 10 ℃ of-20 ℃ of laggard second separating tanks (D202) through the first air cooler (A201) and the first water cooler (EN1) successively, separate hydrogen-rich gas and liquid phase oil product, now, this second separating tank (D202) is in 10 ℃ of-20 ℃ of operations;
3) hydrogen-rich gas that the second separating tank (D202) separates advances circulating hydrogen compressor (K201), be divided into two-way after this circulating hydrogen compressor (K201) pressure-raising, wherein the reforming reaction system of upstream is returned on a road, and another Lu Zejing second air cooler (A202) is cooled to 38 ℃-55 ℃ laggard the 3rd separating tanks (D203), separate gas phase and reformate;
4) gas phase that the 3rd separating tank (D203) separates is advanced after the first supercharger (K202/1) pressure-raising with the liquid phase oil product of contact tank again (D205) from downstream to mix, mixing is cooled to 38 ℃-55 ℃ laggard the 4th separating tanks (D204) by the 3rd air cooler (A203), separates gas and reformate;
5) gas that the 4th separating tank (D204) separates is after the second supercharger (K202/2) pressure-raising, advance successively after the 4th air cooler (A204) and the second water cooler (E203) are cooled to 25 ℃-40 ℃ and mix with the liquid phase oil product from the second separating tank (D202), mix laggard contact tank again (D205), separate hydrogen, now, this again contact tank (D205) in 15 ℃ of-25 ℃ of operations;
6) hydrogen that contact tank (D205) separates again is final to be sent to toward hydrogen pipe network (2), and after coming from the reformate mixing of the 3rd separating tank (D203) and the 4th separating tank (D204), from compressing into the second interchanger (EN2), and after being heated to 60 ℃-85 ℃ with the tower top oil gas of the depentanizer (3) in downstream, with the reformate from the first separating tank (DN1), mix, after mixing from the depentanizer (3) in force feed downstream.
2. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1 is characterized in that: the gas that the liquid phase oil product of described the second separating tank (D202) just separates with the 4th separating tank (D204) after pump (P201AB) pressure-raising mixes.
3. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1 is characterized in that: the hydrogen that described contact tank again (D205) separates advances hydrogen pipe network (2) after the PSA/ film separation unit is purified again.
4. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1, it is characterized in that: described the first water cooler (EN1) is 7 ℃ of cold water water coolers, and its cold water is provided by the lithiumbromide Hot water units.
5. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1, it is characterized in that: described the second water cooler (E203) is water recirculator.
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