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Microactivity test reactor

Figure 2.2.1 shows the simplified sketch of the reactor used for the microactivity test. As can be seen, a fluid-bed catalyst is tested in a fixed bed reactor in the laboratory to predict its performance in a commercial fluid bed reactor. This can be done only because enormous empirical experience exists that has accumulated throughout several decades in several hundreds of reactors both in production and in laboratories. The standard states ... [Pg.33]

Catalytic evaluation of the different pillared clays was performed using a microactivity test (MAT) and conditions described in detail elsewhere (5). The weight hourly space velocity (WHSV) was 14-15 the reactor temperature was 510 C. A catalyst-to-oil ratio of 3.5-3.8 was used. The chargestock s slurry oil (S.O., b.p. >354 C), light cycle oil (LCGO, 232 C < b.p. <354 C) and gasoline content were 62.7 vol%, 33.1 vol% and 4.2 vol% respectively. Conversions were on a vol% fresh feed (FF) basis and were defined as [VfVp/V ] x 100, where is the volume of feed... [Pg.355]

FIXED-BED AND FLUIDIZED-BED TESTS In the fixed-bed test, a sample of cracking catalyst was contacted with an FCC feed in a manner similar to the standard microactivity test (MAT) prescribed by ASTM (10). One major difference was that the reactor temperature was increased from 900°F to 960°F to better simulate current commercial operations. [Pg.102]

Catalytic Cracking Test. A standard microactivity test (MAT) was used to evaluate the conversion and selectivity of catalyst samples. The tests were done at the University of Pittsburgh s Applied Research Center (former Gulf Research Laboratory), a qualified laboratory for MAT evaluations. A standard method, developed by Gulf, was used without modification. A Cincinnati gas oil was cracked under the following conditions cat/oil=3, 16 h 1 WHSV, and 516°C. Prior to charging the reactor, all samples underwent a standard thermal pretreatment. Solids were first heat shocked for 1 h at 593°C. Next, selected materials were impregnated with 3000 ppm Ni and 6000 ppm V, as naphthenates. Then all samples were calcined for 10 h at 538°C. Finally, each material was steamed at 732°C for 14 h in a fluidized bed to produce a catalyst in a simulated equilibrium state. [Pg.420]

D-3907 Method for Testing Fluid Catalytic Cracking Catalysts by Microactivity Test Activity of FCC catalysts as evaluated by percent conversion of gas oil using a fixed bed reactor... [Pg.437]

This paper presents a deactivation model derived from experimental data. A version of the classical microactivity test (MAT) is employed because it is used world-wide to simulate the cracking process, although the contact time is larger than in a riser reactor. [Pg.358]

The Microactivity Test (MAT) reactor is used primarily for cracking catalysts, such as those based on zeolites. In the MAT test, a given amount of feed is pumped within 1-75 s over a measured amount of catalyst in a fixed bed. Liquid and vapor products can be collected separately and analyzed. The MAT and TOS techniques are similar in principle, hence results for these two can be expected to be similar. Comparison with commercial reactors is carried out by empirically adjusting the test conditions. Conversion and simulated distillation results between MAT units can be compared by using standard catalysts and feeds using ASTM D-3907. [Pg.238]

The decrease in the activity of the catalyst is reflected in the lowering of the conversion and impurities removal of the reactant feed to the desired products during time-onstream. It is generally practiced in the refineries that the catalyst is allowed to deactivate to a certain level and, to maintain the production rates within the desired product quality, the reactor temperature is steadily increased to compensate for catalyst deactivation. The level of catalyst deactivation can be measured by comparing the activity of the deactivated catalyst to that of the fresh one. This is, for instance, the approach used in FCC process, in which a microactivity test (MAT) is used to monitor catalyst deactivation by measuring catalyst activity at standard conditions with a standard feedstock. [Pg.494]

An advanced cracking evaluation-automatic production (ACE Model AP) fluidized bed microactivity unit was used to study the catalyst and feed interactions. The fluidized bed reactor was operated at 980°F (800 K). Every feed was tested on two different catalysts at three cat-to-oil ratios 4, 6, and 8. Properties of laboratory... [Pg.186]

While most catalyst vendors rely on fixed bed microactivity (MAT) tests, fixed fluid bed (FFB) reactor experiments are widely used within Mobil to characterize FCC catalysts. The amount of catalyst used is constant for each test, and products are collected for a known period of time. In MAT experiments, catalyst bed is fixed while in FFB test the catalyst bed is fluidized. As products are collected over the decay cycle of the catalyst, the resulting conversion and coke yields are strongly influenced by catalyst deactivation. Systematic differences exist between the measured conversion or catalyst activity and coke yields for the MAT and FFB tests. The magnitude of these differences varies depending on the type of catalyst being tested (REY or USY). Experimental data in Figure 1 clearly show that FFB conversion is higher than MAT conversion for USY catalysts. On the other hand, FFB conversion is lower than MAT conversion for REY catalysts. Furthermore, the quantitative... [Pg.149]

The catalyst used in these tests was a commercial GY-15 (containing 15 wt% of rare earth exchanged 2eolitc Y) with an initial microactivity (MA) of 66 (according to ASTM 3907 method). The feedstocks were a vacuum gas oil (VGO) and an ARO with a Coaradson carbon residue (Ccr) of 4.92. The reactor system and test results are shown in Fig, 2,... [Pg.327]


See other pages where Microactivity test reactor is mentioned: [Pg.198]    [Pg.32]    [Pg.33]    [Pg.163]    [Pg.312]    [Pg.132]    [Pg.353]    [Pg.76]    [Pg.62]    [Pg.62]    [Pg.319]    [Pg.87]   
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