CN103421540B - Oil-gas separation process of catalytic reforming device - Google Patents
Oil-gas separation process of catalytic reforming device Download PDFInfo
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- CN103421540B CN103421540B CN201310345177.0A CN201310345177A CN103421540B CN 103421540 B CN103421540 B CN 103421540B CN 201310345177 A CN201310345177 A CN 201310345177A CN 103421540 B CN103421540 B CN 103421540B
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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 the important means of producing low-carbon (LC) aromatic hydrocarbons and clean gasoline with high octane in oil refining process, simultaneously the important hydrogen source of Ye Shi oil refining enterprise, and it is made up of raw materials pretreatment, reforming reaction, gas-oil separation and product separation four part.Wherein gas-oil separation part carries the task of reforming reaction product separation being become hydrogen-rich gas and reformate, its basic procedure is (as shown in Figure 2): from reforming reactor reaction product first through E0201 with reformer feed namely from the refining petroleum naphtha 01 of pretreatment system and the mixture heat exchange of recycle hydrogen, then enter air cooler A0201 condensing cooling, then enter separating tank D0202 and isolate hydrogen-rich gas and reformate.Wherein, hydrogen-rich gas enters circulating hydrogen compressor K0201, after pressure-raising, one tunnel returns reforming reaction system and participates in reaction, supercharger (K0202/1 and K0202/2) is then entered on another road, mix with the reformate from separating tank D0202 and after pump P0201AB pressure-raising after pressure-raising, through water recirculator E0203 laggard contact tank again D0205, implement to contact again, at low temperature, hydro carbons is wherein adsorbed further by reformate under condition of high voltage, obtain (about 92%) hydrogen that purity is higher, hydrogen pipe network 02 is entered again after directly entering hydrogen pipe network 02 or sending PSA/ film separation unit to purify further, certainly the depentanizer 03 of the product separation part in downstream is compressed into after the isolated reformate of separating tank D0203 and D0204 then mixes.
In above-mentioned flow process, reforming reaction product from E0201 temperature out, directly enters air cooler A0201, not only increases cooling load, also reduce the temperature that reformate enters depentanizer 03, can improve the thermal load of reboiler furnace at the bottom of its tower usually more than 100 DEG C.In addition, because the service temperature of separating tank D0202 is higher, such that the inlet temperature of circulating hydrogen compressor K0201 is higher, recycle hydrogen concentration is low, treatment capacity strengthens, finally cause the steam consumption quantity driving turbine to increase.Therefore, the heat of reforming reaction product secondary is transferred to downstream fractionation system from air cooler A0201, and cooling operation separating tank D0202, the energy consumption for reduction oil and gas separating system and depentanizer is vital, and the present invention puts forward based on these 2 considerations just.
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 separating tank service temperature is higher, cause cooling load large, circulating hydrogen compressor inlet temperature is high, recycle hydrogen concentration is low, treatment capacity is large, reformate enters the low shortcoming of depentanizer temperature, provides a kind of reforming reaction product secondary heat that shifts to derived product separation system and the gas-oil separation technique of catalytic reforming unit realizing 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 reforming reactor reaction product through First Heat Exchanger with from the refining petroleum naphtha of the reforming reaction system of upstream and laggard first separating tank of recycle hydrogen mixture heat exchange, separate gas and reformate;
2) gas that the first separating tank separates is cooled to 10 DEG C-20 DEG C laggard second separating tanks through the first air cooler and the first water cooler successively, and separate hydrogen-rich gas and liquid phase oil product, now, this second separating tank is in 10 DEG C-20 DEG C operations;
3) hydrogen-rich gas that the second separating tank separates enters circulating hydrogen compressor, two-way is divided into after this circulating hydrogen compressor pressure-raising, wherein a road returns the reforming reaction system of upstream, and another Lu Zejing second air cooler is cooled to 38 DEG C-55 DEG C laggard 3rd separating tanks, separates gas phase and reformate;
4) mix with the liquid phase oil product of the contact tank again from downstream after the gas phase that the 3rd separating tank separates enters the first supercharger pressure-raising, be cooled to 38 DEG C-55 DEG C laggard 4th separating tanks through the 3rd air cooler after mixing, separate gas and reformate;
5) gas that separates of the 4th separating tank is after the second supercharger pressure-raising, enter successively after the 4th air cooler and the second water cooler are cooled to 25 DEG C-40 DEG C 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 be in 15 DEG C-25 DEG C operations;
6) the final past hydrogen pipe network of hydrogen that contact tank separates again is sent to, and after coming from the reformate mixing of the 3rd separating tank and the 4th separating tank, from compressing into the second interchanger, and mix with the reformate from the first separating tank, from the depentanizer in force feed downstream after mixing after being heated to 60 DEG C-85 DEG C with the tower top oil gas of the depentanizer in downstream.
The liquid phase oil product gas and vapor permeation that ability and the 4th separating tank separate after pump pressure-raising of described second separating tank.
The hydrogen that described contact tank again separates enters hydrogen pipe network again after PSA/ film separation unit is purified.
Described first water cooler is 7 DEG C of cold water water coolers, and its cold water is provided by lithiumbromide Hot water units.
Described second water cooler is water recirculator.
Compared with prior art, tool has the following advantages and beneficial effect in the present invention:
1, arrange the first separating tank in First Heat Exchanger outlet, and keep gas phase to walk former flow process entering the first air cooler, liquid phase then self-pressure directly removes depentanizer, it reduces the cooling load 9.5 × 10 of reforming reaction product secondary
4kw-4.3 × 10
3kw;
2, the first water cooler is set in the import of the second separating tank, cold water originates from absorption lithiumbromide water-heating cooling unit, hot water is then occurred by device low temperature exhaust heat, it reduce the temperature 12 DEG C-22 DEG C of reformate separating tank, be conducive to the treatment capacity 5422Nm improving recycle hydrogen concentration 2.5%-1.9% and reduce circulating hydrogen compressor
3/ h-5692Nm
3/ h and inlet air temperature 12 DEG C-22 DEG C, thus reduce circulating hydrogen compressor energy consumption 529kw-570kw;
3, be provided with the second interchanger, with the tower top oil gas preheating depentanizer charging of depentanizer, improve the temperature 11.1 DEG C-15.1 DEG C that reformate enters depentanizer, to be conducive to reducing at the bottom of its tower boiling hot load 1.5 × 10 again
3kw-3.0 × 10
3kw;
4, due to needs water-heating cooling, refinery's Low Temperature Thermal trap load 7.88 × 10 is added
3-8.25 × 10
3kw, is conducive to the operation of steady season in summer in winter two hot-water system.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Fig. 2 is the process flow diagram of prior art.
Embodiment
Below in conjunction with multiple specific embodiment, the invention will be further described.
Embodiment 1
Shown in Figure 1, the gas-oil separation technique of the catalytic reforming unit described in the present embodiment, concrete situation is as follows: from reforming reactor reaction product (527 DEG C, 0.316MPag, 273.9t/h) through First Heat Exchanger E201 with from refining petroleum naphtha 1(89 DEG C, 1.0MPag, 242t/h of the reforming reaction system of upstream) and recycle hydrogen (81.7 DEG C, 0.51Mpag, moles of hydrogen concentration 91.8%, 31.8t/h) after mixture heat exchange 104 DEG C enter the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 DEG C) and reformate (76.5t/h, 102 DEG C, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 DEG C) (load of corresponding first air cooler A201 is 1.99 × 10 to be cooled to 50 DEG C through the first air cooler A201
4kw), and then enter this first water cooler of the first water cooler EN1(EN1 and be specially 7 DEG C of cold water water coolers, its cold water is provided by lithiumbromide Hot water units, hot water is then produced by the low temperature exhaust heat of catalytic reforming unit), the load being further cooled to 18 DEG C of corresponding first water cooler EN1 of laggard 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 a water recirculator, the charging of the first water cooler EN1 is cooled to about 32 DEG C before the first water cooler EN1).Now, this second separating tank D202 is in 18 DEG C of lower temperature operation, separates hydrogen-rich gas 235360Nm
3/ h(0.24Mpag, moles of hydrogen concentration 91.8%) and 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 DEG C) after be divided into two-way, a wherein road 125712Nm
3/ h returns the reforming reaction system response of upstream, another road 109648Nm
3/ h enters the second air cooler A202 and is cooled to 50 DEG C (load of corresponding second air cooler A202 is 1.7 × 10
3kw), then enter the 3rd separating tank D203, separate gas phase 109648Nm further
3/ h and reformate (0t/h, 50 DEG C), and the gas phase 109648Nm that the 3rd separating tank D203 separates
3/ h enters the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 DEG C) after, mix 61 DEG C with the liquid phase oil product (20 DEG C, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and enter the 3rd air cooler A203 and be cooled to 50 DEG C (load of corresponding 3rd air cooler A203 is 2.6 × 10
3kw) laggard 4th separating tank D204, separates gas 110822Nm
3/ h and reformate (145.8t/h, 50 DEG C), and the gas 110822Nm that the 4th separating tank D204 separates
3/ h enters the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 DEG C) laggard 4th air cooler A204 is cooled to 50 DEG C (load of corresponding 4th air cooler A204 is 3.9 × 10
3kw) after, then enter this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding second water cooler E203 is 4.0 × 10 to be cooled to 32 DEG C
2kw), after, after being mixed into 25 DEG C with the liquid phase oil product (18 DEG C, 137.7t/h, 2.7MPa) from the second separating tank D202 and after pump P201AB pressure-raising, then enter contact tank D205 again, separate the hydrogen 106880Nm that volumetric molar concentration is 94%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 DEG C) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 again after PSA/ film separation unit is purified, and come from the reformate (0t/h of the 3rd separating tank D203, 50 DEG C) and the reformate (145.8t/h of the 4th separating tank D204, 50 DEG C), mix rear 50 DEG C (145.8t/h) and certainly compress into the second interchanger EN2, with the tower top oil gas (104.6 DEG C of the depentanizer 3 in downstream, 43.3t/h, (load of corresponding second interchanger EN2 is 2.0 × 10 1.0MPa) to be heated 70 DEG C
3and to mix rear 80 DEG C (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of depentanizer 3(in force feed downstream with the reformate (76.5t/h, 102 DEG C, 0.3MPa) from the first separating tank DN1 be 1.05 × 10 kw),
4kw).
Embodiment 2
The gas-oil separation technique of the catalytic reforming unit as different from Example 1 described in the present embodiment, concrete situation is as follows: from reforming reactor reaction product (527 DEG C, 0.316MPag, 273.9t/h) through First Heat Exchanger E201 with from refining petroleum naphtha 1(89 DEG C, 1.0MPag, 242t/h of the reforming reaction system of upstream) and recycle hydrogen (81.7 DEG C, 0.51Mpag, moles of hydrogen concentration 92.2%, 31.8t/h) after mixture heat exchange 104 DEG C enter the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 DEG C) and reformate (76.5t/h, 102 DEG C, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 DEG C) (load of corresponding first air cooler A201 is 1.99 × 10 to be cooled to 50 DEG C through the first air cooler A201
4kw), and then enter this first water cooler of the first water cooler EN1(EN1 and be specially 7 DEG C of cold water water coolers, its cold water is provided by lithiumbromide Hot water units, hot water is then produced by the low temperature exhaust heat of catalytic reforming unit), the load being further cooled to 10 DEG C of corresponding first water cooler EN1 of laggard 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 a water recirculator, the charging of the first water cooler EN1 is cooled to about 32 DEG C before the first water cooler EN1).Now, this second separating tank D202 is in 10 DEG C of lower temperature operation, separates hydrogen-rich gas 235110Nm
3/ h(0.24Mpag, moles of hydrogen concentration 92.2%) and 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 DEG C) after be divided into two-way, a wherein road 125712Nm
3/ h returns the reforming reaction system response of upstream, another road 125462Nm
3/ h enters the second air cooler A202 and is cooled to 38 DEG C (load of corresponding second air cooler A202 is 2 × 10
3kw), then enter the 3rd separating tank D203, separate gas phase 109611Nm further
3/ h and reformate (0t/h, 38 DEG C), and the gas phase 109611Nm that the 3rd separating tank D203 separates
3/ h enters the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 DEG C) after, mix 55 DEG C with the liquid phase oil product (15 DEG C, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and enter the 3rd air cooler A203 and be cooled to 38 DEG C (load of corresponding 3rd air cooler A203 is 3 × 10
3kw) laggard 4th separating tank D204, separates gas 110600Nm
3/ h and reformate (145.8t/h, 38 DEG C), and the gas 110600Nm that the 4th separating tank D204 separates
3/ h enters the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 DEG C) laggard 4th air cooler A204 is cooled to 38 DEG C (load of corresponding 4th air cooler A204 is 4.5 × 10
3kw) after, then enter this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding second water cooler E203 is 2.0 × 10 to be cooled to 32 DEG C
2kw), after, after being mixed into 15 DEG C with the liquid phase oil product (10 DEG C, 137.7t/h, 2.7MPa) from the second separating tank D202 and after pump P201AB pressure-raising, then enter contact tank D205 again, separate the hydrogen 106770Nm that volumetric molar concentration is 94.2%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 DEG C) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 again after PSA/ film separation unit is purified, and come from the reformate (0t/h of the 3rd separating tank D203, 38 DEG C) and the reformate (145.8t/h of the 4th separating tank D204, 38 DEG C), mix rear 38 DEG C (145.8t/h) and certainly compress into the second interchanger EN2, with the tower top oil gas (104.6 DEG C of the depentanizer 3 in downstream, 43.3t/h, (load of corresponding second interchanger EN2 is 2.1 × 10 1.0MPa) to be heated 60 DEG C
3and to mix rear 75 DEG C (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of depentanizer 3(in force feed downstream with the reformate (76.5t/h, 102 DEG C, 0.3MPa) from the first separating tank DN1 be 1.08 × 10 kw),
4kw).
Embodiment 3
The gas-oil separation technique of the catalytic reforming unit as different from Example 1 described in the present embodiment, concrete situation is as follows: from reforming reactor reaction product (527 DEG C, 0.316MPag, 273.9t/h) through First Heat Exchanger E201 with from refining petroleum naphtha 1(89 DEG C, 1.0MPag, 242t/h of the reforming reaction system of upstream) and recycle hydrogen (81.7 DEG C, 0.51Mpag, moles of hydrogen concentration 91.6%, 31.8t/h) after mixture heat exchange 104 DEG C enter the first separating tank DN1, separate gas 265578Nm
3/ h(0.3MPa, 102 DEG C) and reformate (76.5t/h, 102 DEG C, 0.3MPa), and the gas 265578Nm that this first separating tank DN1 separates
3/ h(0.3MPa, 102 DEG C) (load of corresponding first air cooler A201 is 1.99 × 10 to be cooled to 50 DEG C through the first air cooler A201
4kw), and then enter this first water cooler of the first water cooler EN1(EN1 and be specially 7 DEG C of cold water water coolers, its cold water is provided by lithiumbromide Hot water units, hot water is then produced by the low temperature exhaust heat of catalytic reforming unit), the load being further cooled to 20 DEG C of corresponding first water cooler EN1 of laggard 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 a water recirculator, the charging of the first water cooler EN1 is cooled to about 32 DEG C before the first water cooler EN1).Now, this second separating tank D202 is in 20 DEG C of lower temperature operation, separates hydrogen-rich gas 235380Nm
3/ h(0.24Mpag, moles of hydrogen concentration 91.6%) and 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 DEG C) after be divided into two-way, a wherein road 125712Nm
3/ h returns the reforming reaction system response of upstream, another road 109668Nm
3/ h enters the second air cooler A202 and is cooled to 55 DEG C (load of corresponding second air cooler A202 is 1.2 × 10
3kw), then enter the 3rd separating tank D203, separate gas phase 109648Nm further
3/ h and reformate (0t/h, 55 DEG C), and the gas phase 109648Nm that the 3rd separating tank D203 separates
3/ h enters the first supercharger K202/1, pressure-raising is to 1.36Mpag(142 DEG C) after, mix 61 DEG C with the liquid phase oil product (25 DEG C, 2.51Mpag, 147.6t/h) of the D205 of contact tank again from downstream and enter the 3rd air cooler A203 and be cooled to 55 DEG C (load of corresponding 3rd air cooler A203 is 2.0 × 10
3kw) laggard 4th separating tank D204, separates gas 110822Nm
3/ h and reformate (145.8t/h, 55 DEG C), and the gas 110822Nm that the 4th separating tank D204 separates
3/ h enters the second supercharger K202/2, by pressure-raising to 2.59Mpag(118 DEG C) laggard 4th air cooler A204 is cooled to 55 DEG C (load of corresponding 4th air cooler A204 is 3.5 × 10
3kw) after, then enter this second water cooler of the second water cooler E203(E203 and be specially water recirculator) (load of corresponding second water cooler E203 is 4.3 × 10 to be cooled to 32 DEG C
2kw), after, after being mixed into 25 DEG C with the liquid phase oil product (20 DEG C, 137.7t/h, 2.7MPa) from the second separating tank D202 and after pump P201AB pressure-raising, then enter contact tank D205 again, separate the hydrogen 106890Nm that volumetric molar concentration is 93.8%
3/ h(2.51Mpag), now, this again contact tank D205 also can lesser temps (25 DEG C) operation, this hydrogen that contact tank D205 separates again finally send hydrogen pipe network 2 again after PSA/ film separation unit is purified, and come from the reformate (0t/h of the 3rd separating tank D203, 55 DEG C) and the reformate (145.8t/h of the 4th separating tank D204, 50 DEG C), mix rear 55 DEG C (145.8t/h) and certainly compress into the second interchanger EN2, with the tower top oil gas (104.6 DEG C of the depentanizer 3 in downstream, 43.3t/h, (load of corresponding second interchanger EN2 is 2.9 × 10 1.0MPa) to be heated 85 DEG C
3and to mix rear 90 DEG C (222.3t/h) furnace capacity of reboiler furnace at the bottom of the corresponding tower of depentanizer 3(in force feed downstream with the reformate (76.5t/h, 102 DEG C, 0.3MPa) from the first separating tank DN1 be 9.0 × 10 kw),
3kw).
Shown in Figure 2, from reforming reactor reaction product (527 DEG C, 0.316MPag, 281.3t/h) through interchanger E0201 with from refining petroleum naphtha 01(89 DEG C, 1.0MPag, 242t/h of the reforming reaction system of upstream) and recycle hydrogen (101.4 DEG C, 0.51Mpag, moles of hydrogen concentration 89.7%, 39.3t/h) after mixture heat exchange 104 DEG C enter air cooler A0201, being cooled to 50 DEG C of loads entering the corresponding air cooler A0201 of separating tank D0202(is 2.62 × 10
4kw), hydrogen-rich gas 240802Nm is separated
3/ h(0.24Mpag, moles of hydrogen concentration 89.7%) and liquid phase oil product, now, the service temperature of this second separating tank D0202 is 50 DEG C, 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 DEG C) after be divided into two-way, a wherein road 128610Nm
3/ h returns the reforming reaction system response of upstream, another road 112192Nm
3/ h enters air cooler A0202 and is cooled to 50 DEG C (load of corresponding air cooler A0202 is 2.8 × 10
3kw), then enter separating tank D0203 and separate gas phase 112098Nm further
3/ h and reformate (3.2t/h, 50 DEG C), 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 DEG C) after, mix 65 DEG C with the liquid phase oil product (32 DEG C, 2.51Mpag, 213.3t/h) of the D0205 of contact tank again from downstream and enter air cooler A0203 and be cooled to 50 DEG C (load of corresponding air cooler A0203 is 4.0 × 10
3kw) laggard separating tank D0204, separates gas 110948Nm
3/ h and reformate (218.9t/h, 50 DEG C), and the gas 110948Nm that this separating tank D0204 separates
3/ h enters the second supercharger K0202/2, by pressure-raising to 2.59Mpag(118 DEG C) laggard air cooler A0204 is cooled to 50 DEG C (load of corresponding air cooler A0204 is 3.8 × 10
3kw) after, mix 50 DEG C of this water cooler of cooler E0203(E0203 of intaking with the liquid phase oil product (50 DEG C, 203.4t/h, 0.24MPa) from separating tank D0202 and after pump P0201AB pressure-raising and be specially water recirculator) be cooled to 32 DEG C after, then the load entering again the corresponding water cooler E0203 of contact tank D0205(is 1.4 × 10
3kw), the hydrogen 106942Nm that volumetric molar concentration is 93.9% is separated
3/ h(2.51Mpag), this hydrogen that contact tank D0205 separates again finally send hydrogen pipe network 02 again after PSA/ film separation unit is purified, and coming from the reformate (218.9t/h, 50 DEG C) of the reformate (3.2t/h, 50 DEG C) of separating tank D0203 and separating tank D0204, the furnace capacity mixing reboiler furnace at the bottom of the corresponding tower of rear 50 DEG C (222.1t/h) depentanizer 03(from force feed downstream is 1.2 × 10
4kw).
In sum, gas-oil separation technique compared to existing technology, flowage structure aspect of the present invention has set up the first separating tank DN1 and the first water cooler EN1 and the second interchanger EN2(total area is about 290m
2); And energy aspect of the present invention is 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, reduces 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, reduces 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, reduces 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, increases 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, reduces 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, reduces 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, reduces 4.34 × 10
3kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235360Nm
3/ h, reduces 5442Nm
3/ h, corresponding effective power consumption is reduced to 6392kw by 6932kw, reduces 540kw; Meanwhile, 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 compressor total effective power consumption 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 DEG C by 186.6 DEG C before changing, and improve 11.1 DEG C, therefore the furnace capacity of reboiler furnace at the bottom of tower is from 1.2 × 10
4kw is reduced to 1.05 × 10
4kw, reduces 1.5 × 10
3kw.
5) dissolved hydrogen, with reformate entering depentanizer 3 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 declines 4.34 × 10 in the present invention
3kw, total process furnace furnace capacity declines 1.7 × 10
3kw, total compressor effective power consumption decline 585kw, total hydrogen loss reduces 7.2kg/h.Get 90% by standard fuel oil 4000 yuan/t(heater efficiency), the recirculated water 0.3 yuan/t(recirculated water temperature difference gets 8 DEG C), electricity price 0.6 yuan/kwh(Compressor Group total efficiency gets 65%), hydrogen valency 20000 yuan/t calculates, overall running cost reduces by 1466.9 yuan/h, rolls over 1,232 ten thousand yuan/year (working time in device year gets 8400 hours).
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, reduces 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, reduces 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, reduces 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, increases 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, reduces 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, reduces 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, reduces 9.5 × 10
4kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235110Nm
3/ h, reduces 5692Nm
3/ h, corresponding effective power consumption is reduced to 6362kw by 6932kw, reduces 570kw; Meanwhile, 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 compressor total effective power consumption 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 DEG C by 186.6 DEG C before changing, and improve 11.1 DEG C, therefore the furnace capacity of reboiler furnace at the bottom of tower is from 1.2 × 10
4kw is reduced to 1.05 × 10
4kw, reduces 1.5 × 10
3kw.
5) dissolved hydrogen, with reformate entering depentanizer 3 drops to 24.5kg/h by the 32.1kg/h before changing, and reduces 7.4kg/h.
Therefore, comprehensively above-mentioned, in example 2, compared to existing technology, its total cooling load declines 9.5 × 10 in the present invention
3kw, total process furnace furnace capacity declines 1.5 × 10
3kw, total compressor effective power consumption decline 625kw, total hydrogen loss reduces 7.4kg/h.Get 90% by standard fuel oil 4000 yuan/t(heater efficiency), the recirculated water 0.3 yuan/t(recirculated water temperature difference gets 8 DEG C), electricity price 0.6 yuan/kwh(Compressor Group total efficiency gets 65%), hydrogen valency 20000 yuan/t calculates, overall running cost reduces by 1580.9 yuan/h, rolls over 1,328 ten thousand yuan/year (working time in device year gets 8400 hours).
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, reduces 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, reduces 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, reduces 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, increases 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, reduces 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, reduces 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, reduces 4.3 × 10
3kw.
2), the treatment capacity of circulating hydrogen compressor K201 is by 240802Nm
3/ h drops to 235380Nm
3/ h, reduces 5422Nm
3/ h, corresponding effective power consumption is reduced to 6502kw by 6932kw, reduces 529kw; Meanwhile, 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 compressor total effective power consumption 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 DEG C by 186.6 DEG C before changing, and improve 12.1 DEG C, therefore the furnace capacity of reboiler furnace at the bottom of tower is from 1.2 × 10
4kw is reduced to 9.0 × 10
3kw, reduces 3.0 × 10
3kw.
5) dissolved hydrogen, with reformate entering depentanizer 3 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 declines 4.3 × 10 in the present invention
3kw, total process furnace furnace capacity declines 3.0 × 10
3kw, total compressor effective power consumption decline 563kw, total hydrogen loss reduces 5.2kg/h.Get 90% by standard fuel oil 4000 yuan/t(heater efficiency), the recirculated water 0.3 yuan/t(recirculated water temperature difference gets 8 DEG C), electricity price 0.6 yuan/kwh(Compressor Group total efficiency gets 65%), hydrogen valency 20000 yuan/t calculates, overall running cost reduces by 1211.9 yuan/h, rolls over 1,017 ten thousand yuan/year (working time in device year gets 8400 hours).
The examples of implementation of the above are only the preferred embodiment of the present invention, not limit practical range of the present invention with this, therefore the change 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. a gas-oil separation technique for catalytic reforming unit, is characterized in that, comprise the following steps:
1) from reforming reactor reaction product through First Heat Exchanger (E201) with from the refining petroleum naphtha (1) of the reforming reaction system of upstream and laggard first separating tank (DN1) of recycle hydrogen mixture heat exchange, separate gas and reformate, the pressure of this first separating tank (DN1) is 0.3MPa;
2) gas that the first separating tank (DN1) separates is cooled to 10 DEG C-20 DEG C 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 DEG C-20 DEG C operations;
3) hydrogen-rich gas that the second separating tank (D202) separates enters circulating hydrogen compressor (K201), two-way is divided into after this circulating hydrogen compressor (K201) pressure-raising, wherein a road returns the reforming reaction system of upstream, and another Lu Zejing second air cooler (A202) is cooled to 38 DEG C-55 DEG C laggard 3rd separating tanks (D203), separate gas phase and reformate;
4) mix with the liquid phase oil product of the contact tank again (D205) from downstream after the gas phase that the 3rd separating tank (D203) separates enters the first supercharger (K202/1) pressure-raising, be cooled to 38 DEG C-55 DEG C laggard 4th separating tanks (D204) through the 3rd air cooler (A203) after mixing, separate gas and reformate;
5) gas that separates of the 4th separating tank (D204) is after the second supercharger (K202/2) pressure-raising, enter successively after the 4th air cooler (A204) and the second water cooler (E203) are cooled to 25 DEG C-40 DEG C 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) be in 15 DEG C-25 DEG C operations;
6) the final past hydrogen pipe network (2) of hydrogen that contact tank (D205) separates again is sent to, 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 mix with the reformate from the first separating tank (DN1) after being heated to 60 DEG C-85 DEG C with the tower top oil gas of the depentanizer (3) in downstream, from the depentanizer (3) in force feed downstream after mixing.
2. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1, is characterized in that: the liquid phase oil product gas and vapor permeation that ability and the 4th separating tank (D204) separate after pump (P201AB) pressure-raising of described second separating tank (D202).
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 enters hydrogen pipe network (2) again after PSA/ film separation unit is purified.
4. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1, is characterized in that: described first water cooler (EN1) is 7 DEG C of cold water water coolers, and its cold water is provided by lithiumbromide Hot water units.
5. the gas-oil separation technique of a kind of catalytic reforming unit according to claim 1, is characterized in that: described second water cooler (E203) is water recirculator.
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| CN108774545B (en) * | 2018-06-28 | 2020-11-10 | 上海河图工程股份有限公司 | Catalytic reforming re-contact process with cold quantity balance arrangement |
| CN108865251B (en) * | 2018-06-28 | 2020-11-10 | 上海河图工程股份有限公司 | Re-contact process for reducing energy consumption of catalytic reforming device |
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