반응공학1 Youn-Woo Lee School of Chemical and Biological Engineering

반응공학1 Youn-Woo Lee School of Chemical and Biological Engineering
Seoul National University , 599 Gwanangro, Gwanak-gu, Seoul, Korea  

Chap. 1 Mole Balance 反應工學I Seoul National University

Socrates (470-399 B.C.) The first step to knowledge
The first step to knowledge is to know that we are ignorant

Objectives Chapter 1. Mole Balance
After completing Chapter 1, the reader will be able to:  Define the rate of chemical reaction.  Apply the mole balance equations to a batch reactor, CSTR, PFR, and PBR.  Describe two industrial reaction engineering systems.  Describe photos of real reactors. Seoul National University

Chapter 1. Mole Balance 1.1 The Rate of Reaction, -rA
1.2 The General Mole Balance Equation 1.3 Batch Reactors 1.4 Continuous-Flow Reactors 1.4.1 Continuous-Stirred Tank Reactor 1.4.2 Tubular Reactor 1.4.3 Packed-Bed Reactor 1.5 Industrial Reactors 1.5.1 Liquid-phase reaction 1.5.2 Gas-phase reaction Seoul National University

Industrial Reactors Seoul National University

Seoul National University

Batch Reactor Stirring Apparatus
回分式反応器 Batch Reactor Stirring Apparatus Conventional jacket HANDHOLES Seoul National University

flat blade radial turbine
攪拌槽型反應裝置 Cutaway View of CSTR pitched blade turbine Spiral Agitator Turbine Type Impeller flat blade radial turbine Gas Entrainment Impeller Helix Impeller Marine Type Propeller Anchor Stirrer Hydrofoil Seoul National University

攪拌槽型反應裝置 CSTR/batch Reactor Seoul National University

Type of Jacket 攪拌槽型反應裝置 impeller Half pipe jacket Conventional jacket
Baffles Dimpled Jacket Inner coil type Heat exchange impeller Seoul National University

攪拌槽型反應裝置 Stirred Tank Reactor Seoul National University

polymerization reactor
攪拌槽型反應裝置 polymerization reactor Seoul National University

管型反應裝置 High Pressure Tubular Reactor for LDPE (Low Density PolyEthylene) plant ExxonMobil's tubular process technology for Sasol's new high-pressure low density polyethylene (LDPE) plant in Sasolburg, South Africa. The new 220,000 ton-per-year plant is expected to be completed in 2005. Seoul National University

Tubular Reactor for SCWO
管型反應裝置 Tubular Reactor for SCWO The Shinko Pantec Plant, Capacity: 1100 kg/h Seoul National University

a bank of catalyst packed tubes
管型反應裝置 Tubular Reactor for production of ethylbenzene Ethylene Benzene 400oC, 20bar 177oC 510oC a bank of catalyst packed tubes (Zeolite) 430oC, 20bar Ethylbenzene The default configuration catalytically reacts ethylene (reactant A) with benzene (reactant B), an exothermic reaction, to produce ethylbenzene (product C), an intermediate chemical used in the manufacture of styrene monomer. ( Seoul National University

Static Mixer in Tubular Reactor
管型反應裝置 Seoul National University

Industrial Reactor Photos Reactor System Used at Amoco
固定層型反應裝置 Industrial Reactor Photos Reactor System Used at Amoco Seoul National University

“Ultraformer Reactor”-Reforming Petroleum Naphtha
固定層型反應裝置 “Ultraformer Reactor”-Reforming Petroleum Naphtha Spherical Reactors Connected in Series Spherical Reactor at AMOCO Seoul National University

Hydrotreating Unit 固定層型反應裝置
Catalytic hydrotreating is a hydrogenation process used to remove about 90% of contaminants such as nitrogen, sulfur, oxygen, and metals from liquid petroleum fractions. These contaminants, if not removed from the petroleum fractions as they travel through the refinery processing units, can have detrimental effects on the equipment, the catalysts, and the quality of the finished product. Typically, hydrotreating is done prior to processes such as catalytic reforming so that the catalyst is not contaminated by untreated feedstock. Hydrotreating is also used prior to catalytic cracking to reduce sulfur and improve product yields, and to upgrade middle-distillate petroleum fractions into finished kerosene, diesel fuel, and heating fuel oils. In addition, hydrotreating converts olefins and aromatics to saturated compounds. Seoul National University

Fisher-Tropsch synthesis reaction at Sasol Limited Chemical
固定層型反應裝置 Packed Bed Reactor Fisher-Tropsch synthesis reaction at Sasol Limited Chemical Gas inlet (50% conversion) Catalyst K2O/SiO2 on Fe BET=200m2/g Steam injector Tube bundle (2050 tubes) 5cm ID X 12 m H Product = Light hydrocarbon + wax (candle & printing inks) Seoul National University

Straight Though Transport Reactor
流動層型反應裝置 Straight Though Transport Reactor Fisher-Tropsch synthesis reaction at Sasol Limited Chemical Settling hopper Riser (Straight-Through Transport Reactor) (Circulating Fluidized Bed) Standpipe Reactor 3.5 m ID x 38 m H Seoul National University

waxes and distillate fuels
流動層型反應裝置 Straight Though Transport Reactor waxes and distillate fuels catalyst Catalyst 6-9.5 ton/sec Feed 300,000 58% H2 32% CO 9% CH4 1% CO2 Tail Gas (T) 38% H2 35% CH4 12% CO2 11% C2-C5 7% CO Volume=365 m3 3.5m ID X 38m H Synoil 150 ton P=25atm T=350oC Recycle (R) R/T=2 Seoul National University

Sasol Advanced Synthol (SAS) Reactor
流動層型反應裝置 Sasol Advanced Synthol (SAS) Reactor light olefins and gasoline fractions Seoul National University

Fluidized Catalytic Cracking Unit
流動層型反應裝置 Fluidized Catalytic Cracking Unit in the petroleum refining industry Seoul National University

Fluidized Catalytic Cracking Reactor
流動層型反應裝置 Stone & Webster’s plant Seoul National University

Slurry Phase Distillate Reactor
氣泡塔型反應裝置 Slurry Phase Distillate Reactor Seoul National University

For Fischer-Tropsch Reaction
氣泡塔型反應裝置 Bubble Column Reactor For Fischer-Tropsch Reaction Seoul National University

Fluidized Bed Gasification Reactor
流動層型反應裝置 Fluidized Bed Gasification Reactor GTL reactor for Sasol coal-gasified gas into synthetic oil T0512e0a.htm Seoul National University

Residual Oil Fluidized-Bed Catalytic Cracking reactor
流動層型反應裝置 Residual Oil Fluidized-Bed Catalytic Cracking reactor Seoul National University

Dimersol G unit (Two –CSTR and one PFR in series)
管型反應裝置 Dimersol G unit (Two –CSTR and one PFR in series) Institute Français du Petrόle Process Dimerization propylene into isohexanes Seoul National University

Plug-flow reactor for Dimersol™ process
管型反應裝置 Plug-flow reactor for Dimersol™ process The finishing reactor (“the snake”) to comply with LPG specification in the USA (less than 5% olefins) Seoul National University

Automotive Catalytic Converter
固定層型反應裝置 Automotive Catalytic Converter 2NO → N2 + O2 2NO2 → N2 + 2O2 2CO + O2 → 2CO2 Seoul National University

Microreactor and Lab-on-Chip
管型反應裝置 Microreactor and Lab-on-Chip Microreactor made of silicon anodically bonded with glass Lab-on-Chip made of glass and polymer for DNA amplification and detection Rutherford Appleton Laboratory (RAL) in the UK Seoul National University

Microreactor for DNA analysis
管型反應裝置 Microreactor for DNA analysis Seoul National University

Oxidation Reactor in Semiconductor Processing
Seoul National University

Diamond film is synthesized through CVD (Chemical Vapor Deposition)
CVD Diamond coated tools 1 to 2 micron/hour SEM of Diamond Films on Si-wafer substrate Seoul National University

Integrated Circuit Wafer
Metallization bis-hexafluoroacetyl-acetonate-CuII (CF3COCHCF3CO)2Cu Integrated Circuit Wafer and Packaged Device Seoul National University

Chemical Reactions in Microelectronics Processing
Chemical Mechanical Polishing Chemical Vapor Deposition Plasma Etching Electrochemical Deposition Seoul National University

Metal Deposition in Microelectronics Processing
Oxidation reactor silicon-diffusion furnace Metal Deposition Reactor Seoul National University

Ozone Depletion Reaction in Stratosphere
Paul Crutzen (Seoul National University) Mario Molina (MIT) F. Sherwood Rowland (U. C. Irvine) Seoul National University

工業反應裝置分類固定層型反應裝置 (Fixed bed) 移動層型反應裝置 (Moving bed)
流動層型反應裝置 (Fluidized bed) 攪拌槽型反應裝置 (Stirred Tank) 氣泡塔型反應裝置 (Bubble cap tower) 管型反應裝置 (Tubular) 火炎型反應裝置 (Flammed) 氣流型反應裝置 (Pneumatic conveying) 段塔型反應裝置 (Multi-staged) 回轉圓板型反應裝置 (Rotary) Seoul National University

固定層型反應裝置 (Fixed bed) Gas (Liq) Gas inlet Liq Gas Catalyst bed
Gas flow Gas Gas outlet Gas (Liq) Liq (a) Fixed bed (1) (b) Fixed bed (2: Countercurrent) (c) Radial flow type Outlet gas Ammonia + Air Pt/Rh gauze Catalyst bed Pd/Au screen 2 cm Metal mesh Porous bed Support screen Nitric Oxide (d) Parallel flow type (e) Thin bed catalysis reactor (Ammonia Oxidation) Seoul National University

移動層型反應裝置 (Moving bed) Gas Catalyst solid solid Gas Gas Gas Gas Gas
(a) Countercurrent (gas-solid cat. rxn) (b) Countercurrent (gas-solid rxn) (c) Cross flow solid Gas Gas solid solid Gas (d) Moving grid Gas Gas Solid solid Gas solid (e) Rotary kiln (rotated) (f) Multistaged Seoul National University

流動層型反應裝置 (Fluidized bed)
Gas Gas Solid Solid Gas Gas (a) Fluidized bed (gas-solid cat.) (b) Fluidized bed (gas-solid rxn) Gas Gas Gas Flow Liquid Solid Solid Particle Solid Solid Particle Liquid Gas Gas Gas (c) 3 Fluidized bed (d) High flow fluidized bed (e) Spray flow bed Seoul National University

攪拌槽型反應裝置 (Stirred Tank)
Reactant inlet Gas Steam Baffles Liquid Jacket Steam Heat Transfer Coil Impeller Liquid Gas Products outlet (a) CSTR (Jacket) (a) CSTR (Coiled) (c) CSTR (G-L) Products Impeller Reactant inlet Products Reactant inlet (d) Series CSTRs (e) Multi-Staged CSTRs Seoul National University

氣泡塔型反應裝置 (Bubble cap tower)
Gas Gas Gas Liquid Liquid Liquid Heat Transfer Tubes Multi hole plate Ring Sparger Single hole nozzle Gas Liquid Multi hole Gas distributor Gas Liquid Gas Liquid (a) Ring sparger type (b) Single nozzle gas distribution (c) Multi hole gas distribution Seoul National University

管型反應裝置 (Tubular) HT media Reactant inlet Products outlet Jacket
(a) Single tube type Gas Reactant inlet Liquid Gas Liquid Boiler for Steam generation Jacket HT Media Liquid naphtha naphtha preheating tubular reactor tubular reactor burner Cooling water Gas burner HT Media Gas quenching quenching Liquid Liquid Products outlet (b) Multi tube type (c) Burner heated type (d) Wetted wall type (e) Spray tower Seoul National University

段塔型反應裝置 (Multi-staged)
Liquid Gas Rotating Disc Axis Liquid Level Water Vessel 回轉圓板型反應裝置 (Rotary) Gas Liquid Seoul National University

Heat Transfer Mode in Fixed bed catalytic reactor
Gas Gas Catalyst Bed Catalyst Bed Cooling Coils Catalyst Bed adiabatic HT Media Gas Gas Gas Gas (a) Self-heat exchange (b) Multi-tube heat exchange (c) Internal cooler Seoul National University

Heat Transfer Mode in Stirred Tank Reactor
Reflux Condenser HT Media HT Media Heat Exchanger Outer Heat Exchanger Seoul National University

Selection of Reactor Type
G L SC GS GL GLS LL LG SS Fixed bed Moving bed Fluidized bed Stirred tank Bubble cap Tubular Pneumatic Phase Reactor 1 2 3 4 5 6 7 8 9 10 11 12 13 14 G=Gas; phase, L= Liquid phase, SC=Solid catalyst, GS=Gas-Solid phase, GL=Gas-Liquid phase, GLS=Gas-Liquid-Solid phase, LL=Liquid-Liquid phase, LG=Liquid-Gas phase, LS=Liquid-Solid phase, SS=Solid-Solid phase Seoul National University

Selection of Reactor Type 1. Partial Oxidation of Propylene
Ammonia Synthesis Naphtha Reforming Reaction 2. Hydrodesulphurization 3. Immobilized Enzyme Reaction 4. Production of Steel in Furnace 5. Sohio Process for Production of Acrylonitrile Fluidized Catalytic Cracking 6. Gas phase Polymerization of propylene Fluidized Coal Combustion 7. Bulk Polymerization of Styrene 8. Production of Antibiotics 9. Production of Terephthalic Acid Hydrogenation of Edible Oil 10. Emulsion Polymerization of SBR 11. Production of HDPE 12. Liquid phase Oxidation of Olefin 13. Production of Ethylene by Cracking of Naphtha 14. Production of Syngas Seoul National University

Batch Reactor Characteristics No charge or discharge during reaction
Phases Gas, Liquid, Liquid/Solid Application Small scale production Intermediate or one shot production Pharmaceutical Fermentation agricultural chemistry Advantages High conversion per unit volume for one pass Flexibility of operation (same reactor can produce one product one time and a different product the next) Easy to clean Disadvantages High operation cost Product quality can be changed batch to batch Seoul National University

Semi-batch Reactor Characteristics Either one reactant is charged and the other is led continuously (at small concentrations) or else one of the product can be removed continuously to avoid side reaction. Phases Gas/Liquid, Liquid/Solid Application Small scale production Competing reactions Advantages High conversion per unit volume for one run Good selectivity Flexibility of operation (can be used with a reflux condenser for solvent recovery or in bubble type runs) Disadvantages High operation cost Product quality more variable than with continuous operation Seoul National University

Continuous-Stirred Tank Reactor (CSTR)
Characteristics Run at steady state with continuous flow of reactants and products: the feed assumes a uniform composition through the reactor, exit stream has the same composition as in the tank Phases Liquid, Gas/Liquid, Liquid/Solid Application When agitation is required, Series configurations for different concentration streams Advantages Continuous operation Good temperature control Easily adapts to two phase runs Low operating (labor) cost Easy to clean Disadvantages Lowest conversion per unit volume By-passing and channeling possible with poor agitation Seoul National University

Plug Flow Reactor (PFR)
Characteristics One long reactor or many short reactors in a tube bank No radial variation in reaction rate (concentration) Changes with length down the reactor Phases Gas Application Large scale production/Continuous Production Fast reaction High Temperature Advantages High conversion per unit volume Low operating (labor) cost Continuous operation Good heat transfer Disadvantages Undesired thermal gradients Poor temperature control (hot spot) Shutdown and cleaning may be expensive Seoul National University

Packed-Bed Reactor (PBR)
Characteristics Tubular reactor that is packed with solid catalyst Phases Gas/Solid catalyst, Gas/Solid Application Heterogeneous gas phase reaction with a catalyst Advantages High conversion per unit mass of catalyst Low operating (labor) cost Continuous operation Disadvantages Undesired thermal gradients Poor temperature control (hot spot) Channeling Shutdown and cleaning may be expensive Seoul National University

Fluidized-Bed Reactor (PBR)
Characteristics Heterogeneous reaction Like a CSTR in that the reactants are well mixed Phases Gas/Solid catalyst, Gas/Solid Application Heterogeneous gas phase reaction with a catalyst Advantages Good mixing Good uniformity of temperature Catalyst can be continuously regenerated with the use of an auxiliary loop Disadvantages Bed-fluid mechanics are not well known Severe agitation can result in catalyst destruction and dust formation Uncertain scale-up Seoul National University

회분식반응기 (Batch Reactor)
특성 반응이 진행되는 동안에 채우거나 비우지 않음 상 기상, 액상, 액-고상 응용분야 작은 규모의 생산 중간생성물 또는 일회 생산 (One shot production) 의약품 발효 농약 장점 단위 부피당 높은 전환율 청소가 쉬움 운전 유연성 (같은 반응기로 한번은 제품1을 생산하다가 다음 번은 제품2를 생산할 수 있음) 단점 운전비가 높음 제품의 품질이 매회 달라질 수 있음

연속교반조반응기 (CSTR) 특징 반응물/생성물이 연속으로 흐르면서 정상상태로 운전 반응기내의 조성이 일정하게 유지
특징 반응물/생성물이 연속으로 흐르면서 정상상태로 운전 반응기내의 조성이 일정하게 유지 출구 농도는 반응기내의 농도와 동일 상 액상, 기-액, 고-액 응용분야 교반이 필요한 반응 반응기 연속배열 장점 연속운전 온도조절이 용이 2상의 운전이 용이 운전비용이 낮음 청소가 쉬움 단점 단위부피당 낮은 전환율 교반이 불량할 경우 By-passing과 channeling 가능

플러그 흐름반응기 (Plug Flow Reactor: PFR)
특징 연속반응 하나의 긴 튜브반응기 또는 여러 개의 짧은 튜브반응기 뭉치 반경방향으로의 반응속도 (농도) 구배가 없음 반응기 길이를 따라서 반응속도 구배가 존재 상 기상 응용분야 대량생산/연속생산 고속반응 고온 장점 단위부피당 높은 전환율 낮은 운전비용 연속운전 단점 바람직하지 않은 온도구배 발생가능 온도조절이 어려움 (hot spot) 운전정지와 청소가 비쌈

충전층 반응기 (Packed-Bed Reactor: PBR)
특징 고체촉매가 충전된 튜브반응기 상 기-고, 기-고체촉매 응용분야 고체촉매 기상반응 장점 고체촉매무게당 높은 전환율 낮은 운전비용 연속운전 단점 바람직하지 않은 온도구배 발생가능 온도조절이 어려움 (hot spot) 편류(Channeling) 운전정지와 청소가 비쌈

유동층 반응기 (Fluidized-Bed Reactor, FBR)
특징 기-고반응 CSTR과 같이 반응물이 잘 교반 상 기체/고체 촉매, 기체/고체 응용분야 기상 고체촉매반응 장점 우수한 혼합 온도 균일성 유지 부속 장치사용으로 촉매가 연속으로 재생될 수 있음 단점 유체역학 정보가 부족 격한 교반으로 인한 촉매마모 scale-up이 불확실

General Mole Balance on control volume
Seoul National University

Balance on control volume
Nj Gj = rj · V Fj0 Fj A mole balance on species j, at any time, t, yields Rate of flow of j into the system (mole/time) Rate of flow of j out of the system (mole/time) Rate of generation of j by chem. rxn within the system (mole/time) Rate of accumulation of j within the system (mole/time) - + = in out generation = accumulation (1-3) Seoul National University

Rate of formation of species j by chem. rxn
Suppose that the rate of formation of species j for the reaction varies with the position in the control volume. The rate of generation, DGj1, in terms of rj1 and sub-volume DV1 is DV1 DV2 rj1 If the total control volume is divided into M sub-volume, the total rate of generation is rj2 V By taking the limits (i.e., let M →  and DV → 0) and making use of the definition of integral, we can rewrite the foregoing equation in the form r j can have different values at difference locations in the reactor since the properties of the reacting materials (e.g., conc., temp.) Seoul National University

1.2 The General Mole Balance Equation
(GMBE) (1-4) With this GMBE, we can develop the design equations for the various types of industrial reactors: batch, semi-batch, and continuous-flow. Upon evaluation of these equations we can determine the time (batch) or reactor volume (continuous-flow) necessary to convert a specified amount of reactants to products. Seoul National University

The most common industrial reactors
CSTR (backmix reactor) batch reactor Reactants Products PFR (tubular reactor) PBR (packed-bed reactor) Reactants Products Reactants Products Seoul National University

Ideal Reactor Type Batch Reactor
 uniform composition everywhere in the reactor  the composition changes with time Continuous-Stirred Tank Reactor (CSTR)  uniform composition everywhere in the reactor (well mixed)  same composition at the reactor exit Tubular Reactor (PFR)  fluid passes through the reactor with no mixing of earlier and later entering fluid, and with no overtaking.  It is as if the fluid moved in single file through the reactor  There is no radial variation in concentration (plug-flow reactor) Seoul National University

Integrating with limits that
1.3 Batch Reactors If the reaction mixture is perfectly mixed so that there is no variation in the rate of reaction throughout the reactor volume, we can take rj out of the integral and write the GMBE in the form GMBE Design Equation for Batch reactor (1-5) Integrating with limits that at t = 0, NA = NA0 at t = t1, NA = NA1 What time is necessary to reduce the initial number of moles from NA0 to a final desired number NA1? (1-6) Seoul National University

1.3 Batch Reactors A B NB NA t t Fig. 1-6 t1 t1
Moles of A change with time Moles of B increase with time Fig. 1-6 Seoul National University

1.4.1 Continuous-Stirred Tank Reactor (CSTR)
Fj0 GMBE Fj The CSTR is normally run at steady state and is assumed to be perfect mixed. No temporal, spatial variations in conc., temp., or rxn rate throughout the vessel Conc. and temp at exit are the same as they are elsewhere in the tank Non-ideal mixing, residence-time distribution model is needed Design Equation for CSTR (1-7) (1-8) The reactor volume, V, necessary to reduce the entering flow rate from Fj0 to the exit flow rate Fj at reaction rate of rj. (1-9) Seoul National University

Tubular Reactor (PFR) - The reactants are continually consumed as they flow down the length of the reactor - The concentration varies continuously in the axial direction through the reactor. Consequently, the reaction rate will also vary axially. - To develop the PFR design equation, we shall divide (conceptually) the reactor into a number of sub-volumes so that within each sub-volume DV, the reaction rate may be considered spatially uniform. Let Fj(y) represent the molar flow rate of species j into volume DV at y Fj(y+D y) represent the molar flow rate of species j out of volume DV at (y+D y) In a spatially uniform sub-volume DV, Seoul National University

Integrating with limits that
Tubular Reactor (PFR) GMBE in DV (1-10) Integrating with limits that at V = 0, FA = FA0 at V = V1, FA = FA1 Design Equation for PFR (1-11) The reactor volume, V1, necessary to reduce the entering molar flow rate FA0 to some specified value FA1 at reaction rate of rA. (1-13) Seoul National University

1.4.2 Tubular Reactor (PFR) A B FA FB V V
Figure 1-12 profiles of molar flow rates in a PFR Seoul National University

1.4.3 Packed-Bed Reactor (PBR)
For a fluid-solid heterogeneous system, the rate of reaction of a substance A is defined as The mass of solid is used because the amount of the catalyst is what is important to the –r’A (1-14) In out generation = accumulation Design Equation for PBR No pressure drop No catalyst decay Seoul National University

Example 1-2 How large is it? (PFR)
CA0 v0 CA V rA = -kCA The first-order reaction (liquid phase rxn) A  B is carried out in a tubular reactor in which the volumetric flow rate, v0, is constant. (1) Derive an equation relating the reactor volume (V) to the entering concentration of A (CA0), the rate constant k, and the volumetric flow rate v0. (2) Determine the reactor volume necessary to reduce the exiting concentration (CA) to 10% of the entering concentration (CA0) when the volumetric flow rate (v0) is 10 ℓ/min and the specific reaction rate, k, is 0.23 min-1. Seoul National University

Example 1-2 How large is it? (PFR)
GMBE for PFR Tubular, 1st order rxn (1st-order reaction) Combine both side A reactor volume of 100L is necessary to convert 90% of species A entering into product B for the parameter given. Seoul National University

P1-2A How large is it? (CSTR)
V rA=-kCA Fj0 Fj The first-order reaction (liquid phase rxn) A  B is carried out in a CSTR in which the volumetric flow rate, v0, is constant. (1) Derive an equation relating the reactor volume (V) to the entering concentration of A (CA0), the rate constant k, and the volumetric flow rate v0. (2) Determine the reactor volume necessary to reduce the exiting concentration (CA) to 10% of the entering concentration (CA0) when the volumetric flow rate (v0) is 10 ℓ/min and the specific reaction rate, k, is 0.23 min-1. Seoul National University

P1-2A How large is it? (CSTR)
For CSTR, the mole balance on species A was shown to be V rA=-kCA Fj0 Fj The CSTR is almost 4 times larger than the PFR for getting 90% conversion Seoul National University

Mole Balance on Different Reactor
Reactor Differential Algebraic Integral Batch CSTR PFR PBR Seoul National University

종결 이 교과서의 목표는 화학반응공학의 기본원리를 사용하기 쉽고 다양한 문제에 적용할 수 있는 알고리듬 속으로 짜 맞추는 데 있다. 이제 겨우 이러한 알고리듬의 블록 쌓기의 첫 번째 블록인 몰수지를 마쳤다. 몰수지 이 알고리듬과 이 알고리듬의 블록 쌓기의 해당하는 블록들은 다음과 같은 장들에서 전개되고 논의될 것이다:  몰수지 (제1장)  속도법칙 (제3장)  화학양론 (제4장)  결합 (제5장)  계산 (제5장)  에너지수지 (제11장~제13장) 이러한 알고리듬을 사용하여, 우리는 암기보다는 논리에 의해서 화학반응공학 문제들을 접근하고 해결할 수 있다. Seoul National University

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반응공학1 Youn-Woo Lee School of Chemical and Biological Engineering

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