石油炼制设备.docx

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1、Description of Reactors (Petroleum Refining)Multiphase catalytic packed-bed reactors (PBRs) operate in two modes: (1) trickle operation, with a continuous gas phase and a distributed liquid phase, and the main mass transfer resistance located in the gas, and (2) bubble operation, with a distributed

2、gas and a continuous liquid phase, and the main mass transfer resistance located in the liquid phase. For three-phase reactions (gas and liquid phases in contact with a solid catalyst), the common modes of operation are trickle- or packed-bed reactors, in which the catalyst is stationary, and slurry

3、 reactors, in which the catalyst is suspended in the liquid phase (Figure 2. 1). In these reactors, gas and liquid move co-currently down flow or gas is fed countercurrently upflow. Commercially, the former is the most used reactor, in which the liquid phase flows mainly through the catalyst particl

4、es in the form of films, rivulets, and droplets (Figure 2. 2).Based on the direction of the fluid flow, PBRs can then be classified as trickle-bed reactors (TBRs) with co-current gas-liquid downflow, trickle-bed reactors with countercurrent gas-liquid f1ow, and packed-bubble reactors, where gas and

5、liquid are contacted in co-current upflow. To carry out the catalyst and reactor selection and process design properly, knowledge of what each reactor type can and cannot do is very important. When a fixed-bed reactor is chosen, the question frequently asked is whether to use an upflow or downflow m

6、ode of operation.countercurrent operations during hydroprocessing, in which the aforementioned behavior is clearly observededWcneHodnssad -wededWcneHodnssad -wed0.20.40.6ReactantReactor length z,-Figure 2. 4. Profiles of H2S partial pressure along the catalytic bed in an HDT reactor (一, co-current;

7、一, countercurrent). Countercurrent operation provides the highest hydrogen purity in that part of the bed where the least reactive compounds need to be convertedDisadvantagesPresence of flooding at high liquid throughputsEstimation of liquid holdup, pressure drop, and mass transfer coefficients is d

8、ifficult since correlations employed to calculate these parameters do not include data for the small porous catalyst packing typically used in PBRs with two-phase flow Limited to low velocities far below those of industrial interest, due to the occurrence of excessive pressure drop and flooding prob

9、lemsIt is not possible to use smaller (1 to 5 mm) catalyst particles than those used in co-current downflow TBRs High axial dispersion effects in the liquid phasePacked Bubble-Flow Reactors with Co-current Gas-Liquid Upflow This classification includes upflow reactors, upflow co-current reactors, pa

10、cked-bubble columns, upflow packed-bubble columns, and flooded fixed - bed reactors. In bubble-flow operation a continuous liquid phase, together with a dispersed gas phase, move upward co-currently through the packed bed (Figure 2. 1). Such an operation would be recommended in cases where liquid re

11、actants are treated with a relatively small amount of gas, as in the hydration of nitro compounds and olefins, or where a relatively large liquid residence time is required for the degree of conversion desired. Use of these reactors assures complete external wetting of the catalyst and high liquid h

12、oldup. In this mode the liquid is typically the continuous phase.Bubble operation is also advantageous when the reactor diameter/particle diameter ratio is relatively small, because the liquid catalyst contact is more effective than in trickle operation. Compared with empty bubble columns, the packe

13、d bed has the advantage of reducing substantially backmixing in the flowing phases as well as the coalescence of gas bubbles. Under any conditions the wall heat transfer coefficient should also be higher than it is in trickle operation (Hofmann, 1978).For liquid-limited reactions (low liquid reactan

14、t flux to the catalyst particle, high gas reactant flux to the particle), an upflow reactor should be preferred, as it provides complete catalyst wetting and the fastest transport of the liquid reactant to the catalyst. For very shallow catalyst beds, upflow operation gives much better conversions t

15、han down flow operation under the same reaction conditions. The gas and liquid flow rates typically used in a bench-scale down-flow trickle-bed HDS reactor are such that when they are used in co-current upflow operation, a bubble flow regime will be generated.The performance of a reactor under this

16、hydrodynamic flow condition should be considerably different from the one obtained under trickle- f 1 ow conditions. In an upflow system the low-boiling components, which are generally more reactive, pass into the vapor phase and are swept out more rapidly than the high-boiling material, which progr

17、esses relatively slowly through the bed. This superior performance of upflow processing is attributed to the long residence time of the heavy liquid fractions, but a more important factor may be the very low liquid flow used (Satterfield, 1975).When both gas and liquid flow upward, maldistribution o

18、f liquid or incomplete catalyst wetting should not be very important, particularly when the hydrodynamic conditions of bubble flow prevail within the reactor. An upflow (flooded bed) reactor, which should give good solid - iquid contacting, could be used instead of an autoclave to obtain information

19、 on the intrinsic kinetics. The main advantages and disadvantages of TBRs with co-current upflow are given below.AdvantagesRecommended for liquid-limited reactions Liquid holdup is higher. The liquid holdup is larger in an upflow operation than in a downflow operation under similar conditionsBetter

20、effective wetting Better thermal stability for highly exothermic reactionsHigh liquid saturation The liquid flow can be more uniformly distributed (better distribution of liquid throughout the catalyst bed)The gas-liquid and liquid-solid mass transfer coefficients are larger in an upflow operation t

21、han in a downflow operation In backmix flow conditions, where variations in gas and liquid flow rates change the conversion, upflow operation gives better results than down-flow operation under the same conditionsLarger effective residence time If a catalyst gradually becomes deactivated by the depo

22、sit of polymeric or tarry materials, the upflow reactor may maintain its activity longer by washing off these deposits more effectivelyFor rapid and highly exothermic reactions, heat transfer between liquid and solid may also be more effective in upflow than in downflow operationDisadvantagesFor HDT

23、 operations, conversions of sulfur, metals, and asphaltenes decrease with an increase in gas and liquid flow rates at constant temperature and pressure. Conversion of sulfur in upflow operation is reduced faster with time than in downflow operation; however, the conversion is always highest Higher p

24、ump requirements in order to overcome the hydrostatic head of the liquidThe need of some designs to avoid the fluidization of the catalyst unless the catalyst was held in place by an extra weight or suitable mechanical methods If limiting reactant is present in both phases, over a range of operating

25、 conditions in which catalyst pellets filled with liquid are diffusion limited, an upflow reactor wou 1 d be expected to exhibit a lower reaction rate than a partially wetted TBRFormation of stagnant zones inside the catalyst bed Higher axial dispersion compared with the downflow mode of operationSl

26、urry-Bed ReactorsThe best alternative to the use of a fixed - bed reactor with two - phase flow, either upward or downward, is a slurry-bed or ebullating-bed reactor in which the catalyst particles, which must be substantially smaller, are in motion. These reactors are sometimes termed three- phase

27、fluidized - bed reactors or suspended-bed reactors (Figure 2. 1). The main advantages and disadvantages of slurry-bed reactors are given below.AdvantagesHigh heat capacity to provide good temperature control Potentially high reaction rate per unit volume of reactor if the catalyst is highly activeEa

28、sy heat recovery Adaptability to either batch or flow processingMuch lower pressure drop The catalyst may readily be removed and replaced if its working life is relatively shortContinuous removal of solid material formed in reaction Because of high intraparticle diffusion rate, small particles can b

29、e used, which may allow for operating at catalyst effectiveness factors approaching unity, of special importance if diffusion limitations cause rapid catalyst degradation or poorer selectivityLower external mass transfer resistance by means of a high stirring speedDisadvantagesResidence-time distrib

30、ution patterns are close to those of a CSTR, which makes it difficult to obtain high degrees of conversion except by staging and/or increasing operation temperature Generation of fine particles by abrasion of the catalystCatalyst removal by filtration may provoke problems with possible plugging diff

31、iculties on filters, further time of operation, and the costs of filtering systems may be a substantial portion of the capital investment Higher catalyst consumption than that of fixed-bed reactorsDifficult to scale up The high liquid-to-solid ratio in a slurry-bed reactor allows homogeneous side re

32、actions to become more important, if any are possiblePotential hazard of localized overheating in the reactor because of bad fluidization Backmixed f1ow and the volume of the reactor are not fully utilizedLiquidGasLiquidCatalystBubbleCatalyst supportSolid catalystCatalyst supportOutlel collectorSlur

33、ry phasereactorI rickle-bed reactor (3(xmtcr-current flow!7 InletI LJ I1 1 f p (iisinbulor I ray Ceramic ballsTrickle-bed reactor(Co-current flow)Figure 2. 1. Various types of multiphase catalytic reactors.Film flowRivulet flowFilm HowFigure 2. 2. Liquid flow texture found during the trickle-flow re

34、gime in a TBR.Rivulet flowIn the case of catalytic packed beds with two-phase flow, such as those used for straight-run naphtha hydrodesulfurization, from a reactionengineering perspective, a large catalyst-to-liquid volume ratio and plug flow of both phases are preferred, and catalyst deactivation

35、is very s 1 ow or negligible, which facilitates reactor modeling and design. However, for three -phase catalytic reactors such as those employed for hydrotreating of middle distillates and heavy petroleum fractions, the reaction occurs between the dissolved gas and the liquid-phase reactant at the s

36、urface of the catalyst, and the choice of upflow versus downflow operation can be based on rational considerations regarding the limiting reactant at the operating conditions of interest (Dudukovic et al. , 2002).Fixed-Bed ReactorsIn a TBR the catalyst bed is fixed (Figure 2. 1), the flow pattern is

37、 much closer to plug flow, and the ratio of liquid to solid catalyst is small. If heat effects are substantial i. e. , highly exothermic reactions such as those occurring in hydrotreating of unsaturated feeds (light cycle oil from fluid catalytic cracking units) , they can be controlled by recycling

38、 of the liquid product stream, although this may not be practical if the product is not relatively stable under reaction conditions or if very high conversion is desired, as in HDS, since recycling causes the system to approach the behavior of a continuous-stirred-tank reactor (CSTR). For such high-

39、temperature increases, the preferred solution is quenching with hydrogen, although the use of other streams has also been reported. Even when a completely vapor-phase reaction in a fixed catalyst bed may be technically feasible, a TBR may be preferred to save energy costs due to reactant vaporizatio

40、n. The limiting reactant may be essentially all in the liquid phase or in both the liquid and gas phases, and the distribution of reactant and products between the gas and liquid phases may vary with conversion.TBR with Co-current Gas-Liquid Downflow A TBR consists of a column that may be very high

41、(above 10 to 30 m), equipped with one or various fixed beds of solid catalysts, throughout which gas and liquid move in co-current downflow. Figure 2. 3 shows the typical film flow texture found during a trickle-flow regime (Gianetto and Specchia, 1992). In this mode, gas is the continuous phase and

42、 liquid holdup is lower. This operation is the one most used in practice, since there are less severe limitations in throughput than in countercur-rent operation.For gas-limited reactions (high liquid reactant flux to the catalyst particle, low gas reactant flux to the particle), especially at parti

43、ally wetted conditions, a downflow reactor is preferred, as it facilitates transport of the gaseous reactant to the catalyst (Dudukovic et al. , 2002). In contrast to commercial TBR, in the case of bench-scale TBR operating at equivalent space velocity, the liquid velocity and the catalyst bed lengt

44、h have important effects on the performance of the reactor. The principal advantages and disadvantages of TBR with downflow co-current operation are given below.AdvantagesRecommended for gas-limited reactions Liquid flow approaches plug-flow behavior, which leads to high conversionsH yctrocarhonfeed

45、I iquid Gas_ru-xx _l / StagnanlCavityLiquid Offgas productGasReactoroutletFigure 2. 3. Nonideal TBR suffering from liquid maldistribution. Low liquid-solid volume ratio: fewer occurrences of homogeneous side reactionsPossibility of varying the liquid rate according to catalyst wetting and heat and m

46、ass transfer resistances A variety of flow regimes allowed; most flexible with respect to varying throughput demandsThe down f1ow mode also helps keep the bed in place, although with catalysts that are soft or deformable, this might hasten undesired cementation Compared with countercurrent flow oper

47、ation, for co-current flow of the two phases, no limitation on the throughput arises from the phenomenon of flooding, and the quantities of the phase that can be passed depend only on the upstream pressure available because of vaporization effectsAt higher gas loadings, the texture of the liquid is

48、modified by gas-phase friction, the liquid distribution is improved (lower liquid wall flow), and the pressure drop rises (less rapidly in co-current than in countercurrent f1ow) Easy operation with fixed adiabatic beds; for exothermic reaction systems, gas or liquid streams as quench, and the liqui

49、d and/or gas recycle limit temperature risesPossibility of operating at higher pressure and temperature Pressure drop through the bed is relatively low, thus reducing pumping costsLarger reactor size, and generally of simple construction, as there are no moving parts Lower investment and operating costs, and low catalyst los