CN105331389A - Reforming heat recycling technology and device - Google Patents
Reforming heat recycling technology and device Download PDFInfo
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- CN105331389A CN105331389A CN201510915252.1A CN201510915252A CN105331389A CN 105331389 A CN105331389 A CN 105331389A CN 201510915252 A CN201510915252 A CN 201510915252A CN 105331389 A CN105331389 A CN 105331389A
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Abstract
The invention provides a reforming heat recycling technology and device. The technology comprises the steps of recycling top oil gas heat of a depentanizer, strengthening heat exchange of fed materials of the depentanizer and base oil of the depentanizer and improving heat exchange of the base oil of the depentanizer and fed materials of a debutanizer. The invention further provides the reforming heat recycling device, wherein cold low-separated oil and hot low-separated oil of a reaction oil gas separating unit are connected with a feeding port of the depentanizer through a heat exchange unit, and top oil of the depentanizer is connected with a feeding port of the debutanizer through the heat exchange unit. According to the reforming heat recycling technology and device, the temperature of the fed materials of the depentanizer and the debutanizer can be increased, and the load of a reboiling furnace at the bottom of the depentanizer and the heating load of the bottom of the debutanizer are reduced; compared with the prior art, fuel consumption of the depentanizer can be reduced by 10%-20%, steam consumption of the debutanizer can be reduced by about 10%-30%, and the obvious energy saving effect is achieved.
Description
Technical field
The present invention relates to oil-refining chemical production field, especially relate to a kind of reformation heat recovery and utilization technique and device.
Background technology
Reformer belongs to oil refining secondary processing device, main with raw materials such as low-octane virgin naphtha, hydrotreated naphthas, under catalyzer and certain pressure, temperature condition, there is reforming reaction, produce high-octane reformed gasoline, and by-product hydrogen, reformed gasoline can be used as aroamtic hydrocarbon raw material, or as gasoline blending component.
The reformer technological process of production comprises raw materials pretreatment, reforming reaction, reaction oil gas separation, product fractionation and catalyst regeneration five unit.Wherein reaction oil gas is separated and product fractionation process flow process is: reforming reaction product through with catalytic reforming feedstock heat exchange after, then to be cooled by air-cooler and water recirculator, enter reforming reaction product and divide flow container, carry out gas-liquid separation.Divide flow container gas phase to divide two-way, wherein a road is after circulating hydrogen compressor compression, returns reforming reaction unit as recycle hydrogen; Another road is after hydrogen booster supercharging, air-cooler cooling, and point flow container liquid phase after pressurizeing through pump mixes again.Mixed gas-liquid two-phase through unit cooler refrigeration, enters contact tank again and carries out gas-liquid separation again, and tank deck gas phase is attached most importance to whole hydrogen, enters hydrogen pipe network or hydrogen upgrading unit.Again liquid phase at the bottom of contact tank successively with to contact at the bottom of charging, depentanizer oil heat exchange again after, enter depentanizer.Depentanize tower top oil gas is after cooling, and enter return tank and carry out gas-liquid separation, gas phase enters gas pipe network, liquid phase through pressurization rear section as backflow, part through with heat exchange oily at the bottom of debutanizing tower after enter debutanizing tower, isolate petroleum naphtha and liquefied gas component.At the bottom of depentanizer oil with charging heat exchange after, through cooling after deliver to tank field, as reformed gasoline product, or without cooling directly enter dehexanizing column, isolate C
6component is as aromatics extraction raw material.At the bottom of debutanizing tower oil with charging heat exchange after, through cooling after deliver to tank field, as petroleum naphtha product.At the bottom of depentanizer, institute's heat requirement is provided by reboiler furnace, and at the bottom of debutanizing tower, institute's heat requirement is provided by 1.0MPa steam.
Above-mentioned technical process also exists several irrational energy process, and one is that reformed oil exists the process repeatedly cooling-heat; Two be depentanizer charging directly and heat exchange at the bottom of tower, feeding temperature is on the low side; Three is that depentanize tower top oil gas directly cools, and heat is not recycled; Four be debutanizing tower charging only with oil heat exchange at the bottom of tower, feeding temperature is on the low side.
CN103725306A discloses a kind of separation method and device of reforming reaction product, comprise the following steps: after reforming reaction product and reforming reaction charging heat exchange, directly enter the pre-separation tank set up, pre-separation gas phase enters follow-up separating tank and contact part more again after air cooling cooling, isolate recycle hydrogen and high-purity hydrogen, pre-separation liquid phase then with after contact tank liquid-phase mixing more directly enters follow-up fractionating section.By arranging B-grade condensation separating step, decreasing the flow repeating cooling, intensification logistics, reducing the heating load of fractionating section, alleviate the contradiction of air cooling underload in summer simultaneously, compared with prior art, the present invention reduces cooling load 14.5%, reduces heating load 18.2%.
Above-mentioned open invention is only optimized design to reformation reaction oil gas separating unit, not being optimized design to product fractionation unit, to how reducing fractionating section heating load not being described.The present invention, on this invention basis, by optimizing the heat exchange process of fractionation unit, not only make use of the heat that low point of heat is oily, also reclaiming the heat that make use of fractionation tower top oil gas, improve separation column feeding temperature, thus reduce heating load at the bottom of the tower of separation column.
Summary of the invention
For solving the problems referred to above of prior art, the invention provides a kind of reformation heat recovery and utilization technique and device, by described technique and device, the heat that low point of heat is oily can be utilized, and fully reclaim the heat of depentanize tower top oil gas, reduce tower top cooling load, strengthen heat exchange at the bottom of depentanizer charging and tower simultaneously, increase oil at the bottom of depentanizer and debutanizing tower charging heat exchange process, thus reduction heat transfer temperature difference, improve depentanizer and debutanizing tower feeding temperature, reduce thermal load at the bottom of tower, there is obvious energy-saving effect.
For reaching this object, the present invention by the following technical solutions:
First aspect, the invention provides a kind of reformation heat recovery and utilization technique, described technique comprises the heat recycling depentanize tower top oil gas, the heat exchange strengthening oil at the bottom of depentanize charging and depentanizer and increases oil at the bottom of depentanizer and debutanizing tower charging heat exchange.
In the present invention, described technique comprises key step: from cold low point of oil and the heat exchange of depentanize tower top oil gas of reforming reaction separating unit, mix with low point of the heat of reforming reaction separating unit oil again, mixed solution again with heat exchange oily at the bottom of depentanizer, finally enter depentanizer; At the bottom of depentanizer oil with depentanizer charging heat exchange after, then with debutanizing tower charging heat exchange; Depentanize overhead oil first with oil heat exchange at the bottom of depentanizer, then with oil heat exchange at the bottom of debutanizing tower, finally enter debutanizing tower.
In the present invention, described depentanizer charging, from reforming reaction separating unit, comprises heat low point of oil and cold low point of oil.
In the present invention, described heat low point of oil and cold low point of oil are separated by condensed in two stages and obtain, and heat low point of oil temperature is 80-120 DEG C, and cold low point of oil temperature is 30-50 DEG C.
In the present invention, the feeding temperature of described depentanizer is 150-200 DEG C, and column bottom temperature is 200-250 DEG C.
In the present invention, the feeding temperature of described debutanizing tower is 80-120 DEG C, and column bottom temperature is 100-150 DEG C.
As the present invention's preferred technical scheme further, described technique specifically comprises the following steps: after reforming reaction product and catalytic reforming feedstock heat exchange, first carry out a gas-liquid separation without cooling, isolated liquid phase is heat low point of oil, and isolated gas phase carries out secondary gas-liquid separation again after cooling; Liquid phase after secondary separation is cold low point of oil, and isolated gas phase comprises recycle hydrogen and reformation hydrogen.After cold low point of oil and the heat exchange of depentanize tower top oil gas, then mix with low point of heat oil, mixed solution again with heat exchange oily at the bottom of depentanizer, enter depentanizer afterwards; At the bottom of depentanizer oil with depentanizer charging heat exchange after, then with debutanizing tower charging heat exchange, after through cooling after deliver to tank field, as reformed gasoline product; Depentanize tower top oil gas through with cold low point of oily heat exchange after, then to be separated with separatory through cooling, liquid phase part (overhead oil) first with heat exchange oily at the bottom of depentanizer, then with heat exchange oily at the bottom of debutanizing tower, finally enter debutanizing tower; Oil at the bottom of debutanizing tower and debutanizing tower charging heat exchange, then tank field is delivered to, as petroleum naphtha product after cooling.
Second aspect, present invention also offers a kind of reformation device for recycling heat, it comprises the reforming reaction gas-oil separation unit and fractionation unit that connect successively, described fractionation unit comprises the depentanizer and debutanizing tower that connect successively, wherein the opening for feed of depentanizer is connected by cold low point of oil of heat exchange unit and reforming reaction gas-oil separation unit and low point of heat oil, and depentanizer overhead oil is connected with the opening for feed of debutanizing tower by heat exchange unit.
In device of the present invention, cold low point of oil of described reforming reaction gas-oil separation unit by after the interchanger of depentanizer top, then mixes with low point of heat oil, then is connected with the opening for feed of depentanizer through depentanizer feed exchanger.
In device of the present invention, described depentanize overhead oil interchanger, debutanizing tower charging-Ta end interchanger at the bottom of debutanizing tower charging-depentanizer are connected with the opening for feed of debutanizing tower.
Device of the present invention, it is for implementing aforementioned described reformation heat recovery and utilization technique.
Particularly, according to a kind of specific embodiments of the present invention, cold low point of oil and depentanize tower top oil gas heat exchange to 50 ~ 80 DEG C, then mix with low point of heat oil, mixed solution (60 ~ 90 DEG C) again with at the bottom of depentanizer oil heat exchange to 150 ~ 200 DEG C, enter depentanizer afterwards; At the bottom of depentanizer oil with depentanizer charging heat exchange after, then with debutanizing tower charging heat exchange to 80 ~ 120 DEG C, after through cooling after deliver to tank field, as reformed gasoline product; Depentanize tower top oil gas through with cold low point of oily heat exchange after, then to be separated with separatory through cooling, liquid phase part (overhead oil) first with heat exchange oily at the bottom of depentanizer, then with heat exchange oily at the bottom of debutanizing tower after to 80 ~ 120 DEG C, enter debutanizing tower; Oil at the bottom of debutanizing tower and debutanizing tower charging heat exchange, then tank field is delivered to, as petroleum naphtha product after cooling.
Compared with prior art, the present invention at least has following beneficial effect:
The present invention is by being optimized the heat exchange process of reformer product fractionation unit, recycle the heat of depentanize tower top oil gas, strengthening depentanizer charging and the heat exchange at the bottom of tower, and increase oil at the bottom of depentanizer tower and debutanizing tower charging heat exchange, the heat of high temperature of oil at the bottom of depentanizer can be made full use of, improve the feeding temperature of depentanizer and debutanizing tower, reduce the heating load of depentanizer and debutanizing tower; Compared with prior art, reduce depentanizer about fuel consumption 10%-20%, reduce debutanizing tower steam consumption 10-30%, there is obvious energy-saving effect.
Accompanying drawing explanation
Fig. 1 is the reformation heat recovery and utilization process flow sheet of the embodiment of the present invention 1;
Wherein, 1-depentanizer charging-Ta end interchanger, 2-depentanizer, interchanger at the bottom of 3-debutanizing tower charging-depentanizer, air cooler at the bottom of 4-depentanizer, water cooler at the bottom of 5-depentanizer, 6-cold low point of oil-depentanizer top interchanger, 7-depentanizer head space cooler, 8-depentanize tower top water cooler, 9-depentanize return tank of top of the tower, 10-debutanizing tower charging-Ta end interchanger, 11-debutanizing tower, water cooler at the bottom of 12-debutanizing tower.
Embodiment
For ease of understanding the present invention, it is as follows that the present invention enumerates embodiment.Those skilled in the art should understand, described embodiment is only help to understand the present invention, should not be considered as concrete restriction of the present invention.
Embodiment 1
For certain refinery 1,200,000 tons/year of reformers, illustrate that the present invention reforms heat recovery and utilization method.
Technical process of the prior art is:
From reforming reaction gas-oil separation unit depentanizer charging (40 DEG C, main C
5-C
10component) enter depentanizer charging-Ta end interchanger 1, with oil heat exchange to 165 DEG C at the bottom of depentanizer, enter depentanizer 2.Depentanize tower top oil gas (110 DEG C, C
5following component) enter air cooler 7, water cooler 8, be cooled to 40 DEG C, enter return tank 9 and carry out gas-liquid separation, gas phase enters gas pipe network, liquid phase is through the backflow of pressurization rear section, and part enters debutanizing tower charging-Ta end interchanger 10, with oil heat exchange to 75 DEG C at the bottom of debutanizing tower, enter debutanizing tower 11, isolate petroleum naphtha and liquefied gas component.Oil at the bottom of depentanizer (214 DEG C) enters depentanizer charging-Ta end interchanger 1, with depentanizer charging heat exchange to 93 DEG C, then enters air cooler 4, water cooler 5, delivers to tank field through being cooled to 40 DEG C.Oil at the bottom of debutanizing tower (140 DEG C) enters debutanizing tower charging-Ta end interchanger 10, after debutanizing tower charging heat exchange, then enters water cooler 12, is cooled to 40 DEG C and delivers to tank field.Adopt reboiler furnace as thermal source at the bottom of depentanizer, heating load is 7353kW, and adopt 1.0MPa steam as thermal source at the bottom of debutanizing tower, heating load is about 1063kW.
The device of the present embodiment comprises the depentanizer 2 and debutanizing tower 11 that connect successively, wherein, cold low point of oil of reforming reaction gas-oil separation unit is by after depentanizer top interchanger 6, a point oil export low with heat is connected again, be connected with the opening for feed of depentanizer through depentanizer charging-Ta end interchanger 1 again, the tower top of depentanizer connects cold low point of oil-depentanizer top interchanger 6 successively, depentanizer head space cooler 7, depentanize tower top water cooler 8 and depentanize return tank of top of the tower 9, and by interchanger 3 at the bottom of debutanizing tower charging-depentanizer, at the bottom of debutanizing tower charging-debutanizing tower, interchanger 10 is connected with the opening for feed of debutanizing tower 11, interchanger 3 at the bottom of depentanizer charging-Ta end interchanger 1 and debutanizing tower charging-depentanizer successively at the bottom of the tower of depentanizer, be connected with air cooler 4 and water cooler 5 again, be connected with water cooler 12 through debutanizing tower charging-Ta end interchanger 10 at the bottom of debutanizing tower.
The technical process of employing the present embodiment is:
Cold low point of oil (40 DEG C) from reforming reaction gas-oil separation unit enters depentanizer top interchanger, with the heat exchange to 60 DEG C of depentanize tower top oil gas, point oil low with heat (100 DEG C) mixes again, mixed solution (70 DEG C) enters depentanizer charging-Ta end interchanger 1 again, with oil heat exchange to 175 DEG C at the bottom of depentanizer, enter depentanizer 2.Depentanize tower top oil gas (100 DEG C) is introduced into cold low point of oil-depentanizer top interchanger 6, after cold low point of oily heat exchange to 90 DEG C, enter air cooler 7, water cooler 8 again, be cooled to 40 DEG C, enter return tank 9 and carry out gas-liquid separation, gas phase enters gas pipe network, liquid phase is through the backflow of pressurization rear section, part enters debutanizing tower charging-Ta end interchanger 3, with oil heat exchange to 70 DEG C at the bottom of debutanizing tower, then enter interchanger 10 at the bottom of debutanizing tower charging-depentanizer, with oil heat exchange to 95 DEG C at the bottom of depentanizer, enter debutanizing tower 11, isolate petroleum naphtha and liquefied gas component.Oil at the bottom of depentanizer (214 DEG C) enters depentanizer charging-Ta end interchanger 1, with depentanizer charging heat exchange to 100 DEG C, enter interchanger 3 at the bottom of debutanizing tower charging-depentanizer again, with debutanizing tower charging heat exchange to 90 DEG C, entering air cooler 4, water cooler 5 again, delivering to tank field through being cooled to 40 DEG C.Oil at the bottom of debutanizing tower (140 DEG C) enters debutanizing tower charging-Ta end interchanger 10, after debutanizing tower charging heat exchange, then enters water cooler 12, is cooled to 40 DEG C and delivers to tank field.Adopt reboiler furnace as thermal source at the bottom of depentanizer, heating load is 5994kW, and adopt 1.0MPa steam as thermal source at the bottom of debutanizing tower, heating load is about 784kW.
Before and after optimizing, separation column cooling load and heating load change as shown in table 1 below.
Table 1
As seen from the above table, adopt technique of the present invention, can reduce depentanizer heating load 18.5%, reduce debutanizing tower heating load 26.2%, tower top cooling load is substantially constant, has obvious energy-saving effect.
Applicant states, the present invention illustrates detailed process equipment and process flow process of the present invention by above-described embodiment, but the present invention is not limited to above-mentioned detailed process equipment and process flow process, namely do not mean that the present invention must rely on above-mentioned detailed process equipment and process flow process and could implement.Person of ordinary skill in the field should understand, any improvement in the present invention, to equivalence replacement and the interpolation of ancillary component, the concrete way choice etc. of each raw material of product of the present invention, all drops within protection scope of the present invention and open scope.
Claims (10)
1. a reformation heat recovery and utilization technique, is characterized in that, described technique comprises the heat recycling depentanize tower top oil gas, the heat exchange strengthening oil at the bottom of depentanize charging and depentanizer and increases oil at the bottom of depentanizer and debutanizing tower charging heat exchange.
2. technique according to claim 1, it is characterized in that, described technique comprises following steps: from cold low point of oil and the heat exchange of depentanize tower top oil gas of reforming reaction gas-oil separation unit, mix with low point of the heat oil of reforming reaction gas-oil separation unit again, mixed solution again with at the bottom of depentanizer oil heat exchange, finally enter depentanizer; At the bottom of depentanizer oil with depentanizer charging heat exchange after, then with debutanizing tower charging heat exchange; Depentanize overhead oil first with oil heat exchange at the bottom of depentanizer, then with oil heat exchange at the bottom of debutanizing tower, finally enter debutanizing tower.
3. technique according to claim 1 and 2, is characterized in that, described depentanizer charging, from reforming reaction gas-oil separation unit, comprises heat low point of oil and cold low point of oil.
4. the technique according to any one of claim 1-3, is characterized in that, described heat low point of oil and cold low point of oil are separated by condensed in two stages and obtain, and heat low point of oil temperature is 80-120 DEG C, and cold low point of oil temperature is 30-50 DEG C.
5. the technique according to any one of claim 1-4, is characterized in that, the feeding temperature of described depentanizer is 150-200 DEG C, and column bottom temperature is 200-250 DEG C;
Preferably, the feeding temperature of described debutanizing tower is 80-120 DEG C, and column bottom temperature is 100-150 DEG C.
6. the technique according to any one of claim 1-5, it is characterized in that, described technique specifically comprises the following steps: after reforming reaction product and catalytic reforming feedstock heat exchange, a gas-liquid separation is first carried out without cooling, isolated liquid phase is heat low point of oil, and isolated gas phase carries out secondary gas-liquid separation after cooling; Liquid phase after secondary separation is cold low point of oil, and isolated gas phase comprises recycle hydrogen and reformation hydrogen; After cold low point of oil and the heat exchange of depentanize tower top oil gas, then mix with low point of heat oil, mixed solution again with heat exchange oily at the bottom of depentanizer, enter depentanizer afterwards; At the bottom of depentanizer oil with depentanizer charging heat exchange after, then with debutanizing tower charging heat exchange, after through cooling after deliver to tank field, as reformed gasoline product; Depentanize tower top oil gas through with cold low point of oily heat exchange after, then to be separated with separatory through cooling, liquid phase part first with heat exchange oily at the bottom of depentanizer, then with heat exchange oily at the bottom of debutanizing tower, finally enter debutanizing tower; Oil at the bottom of debutanizing tower and debutanizing tower charging heat exchange, then tank field is delivered to, as petroleum naphtha product after cooling.
7. a reformation device for recycling heat, it is characterized in that, it comprises the reforming reaction gas-oil separation unit and product fractionation unit that connect successively, described product fractionation unit comprises the depentanizer and debutanizing tower that connect successively, wherein the opening for feed of depentanizer is connected by cold low point of oil of heat exchange unit and reforming reaction gas-oil separation unit and heat low point of oil-in, and depentanizer overhead oil is connected with the opening for feed of debutanizing tower by heat exchange unit.
8. device according to claim 7, is characterized in that, cold low point of oil of described reforming reaction gas-oil separation unit by after the interchanger of depentanizer top, then mixes with low point of heat oil, then is connected with the opening for feed of depentanizer through depentanizer feed exchanger.
9. device according to claim 7, is characterized in that, described depentanize overhead oil interchanger at the bottom of depentanizer charging-Ta end interchanger, debutanizing tower charging-debutanizing tower is connected with the opening for feed of debutanizing tower.
10. device according to claim 7, it is for implementing the claims the technique described in any one of 1-6.
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