Mass-flow controller

Liquid mass flow controller LCA-42-2-C-1 Porter Instr. 

At the time of the solvent methanol experiments a metering pump was used. In some experiments the pulsating action of the pump can be disturbing, so a high-pressure syringe-type pump can be used. Since mass flow controllers are available now, the combination of a gas-pressurized feed tank on an electronic scale for liquid level indication and a mass flow controller seems to be a good choice. Both the feed tank and separator can be heated or cooled. In the case of the solvent methanol experiments. 

The unit shown on the next page in figure 4.4.1 is a somewhat simplified version of a tested, actual unit. The six gaseous feed components enter through check valves at a pressure regulated to about 4 atm higher pressure then experimental pressure, e.g., 22 atm. Six mass flow controllers set the flows and all but the nitrogen lines are secured with power to open solenoid valves (SV). 

These conditions are usual for modern gas flow programming devices that utilize mass flow controllers which are often computer operated. Now, if (AV(o)) is an... 

Figure 12-26. The SIMULAR reaction calorimeter. Features include pumped liquid feed, gas mass flow control, gas evolution measurement, and distillation equipment. (Source Hazard Evaluation Laboratory Ltd.)...

Figure 12.17 Schematic diagrams of solvent-flush systems, (a) Dual-column MCS unit, which is positioned prior to the first column (C 1) flushing is earned out with both NV 1 and MFC 2 open, (b) Dual-column DCS unit solvent flushing is carried out via the splitline, with MFC 3 open (NV, needle valve MFC, mass flow control). Reprinted with permission from Ref. (20).

Gases. The reactants (including diluent, extender, and carrier gases) must be transported and metered in a controlled manner into the reactor. In the case of gaseous reactants, this does not present any particular problem and is accomplished by means of pressure controllers, gauges, flowmeters, and mass-flow controllers. 

Another delivery system is shown in Fig. 5.4, where a mass-flow controller injects a carrier gas into a heated bubbler. The carrier gas becomes saturated with the reactant vapor, which is then carried into the deposition chamber through a pressure controller and flowmeter.C]... 

Figure 5.4. Bubbler with mass-flow controller.

Drexel, C. F., Digital Mass Flow Controller Come of AgeJ Solid State Technology, pp. 99-106 (Nov. 1996)... 

The oxygen feed to the reactor is controlled using Brooks 5850E Series mass flow controllers. Aqueous HBr is delivered to the reactor system using Harvard... 

The schematic diagram of the experimental setup is shown in Fig. 2 and the experimental conditions are shown in Table 2. Each gas was controlled its flow rate by a mass flow controller and supplied to the module at a pressure sli tly higher than the atmospheric pressure. Absorbent solution was suppUed to the module by a circulation pump. A small amount of absorbent solution, which did not permeate the membrane, overflowed and then it was introduced to the upper part of the permeate side. Permeation and returning liquid fell down to the reservoir and it was recycled to the feed side. The dry gas through condenser was discharged from the vacuum pump, and its flow rate was measured by a digital soap-film flow meter. The gas composition was determined by a gas chromatograph (Yanaco, GC-2800, column Porapak Q for CO2 and (N2+O2) analysis, and molecular sieve 5A for N2 and O2 analysis). The performance of the module was calculated by the same procedure reported in our previous paper [1]. 

Catalytic activity for the selective oxidation of H2S was tested by a continuous flow reaction in a fixed-bed quartz tube reactor with 0.5 inch inside diameter. Gaseous H2S, O2, H2, CO, CO2 and N2 were used without further purification. Water vapor (H2O) was introduced by passing N2 through a saturator. Reaction test was conducted at a pressure of 101 kPa and in the temperature range of 150 to 300 °C on a 0.6 gram catalyst sample. Gas flow rates were controlled by a mass flow controller (Brooks, 5850 TR) and the gas compositions were analyzed by an on-line gas chromotograph equipped with a chromosil 310 coliunn and a thermal conductivity detector. 

Air was supplied from a compressor, moisture and particles in the air are removed passing a trap, and air flow rate was controlled by mass flow controller (5850E, Brooks Co.). The dry sorbents after the attrition were collected, then the particle sizes of them were measured by... 

An experimental fluidized bed reactor has a 2.5 cm in diameter and 230 cm in height, and the distributor has 32 holes and each hole was 2 mm in diameter. 200 mesh net was put on the distributor to prevent particles from falhng down. The cyclone was made by standard proportion to collect fine particles. Air flow rate was controlled by a flow meter, CO2 (99.9%) flow rate was controlled by mass flow controller and then 10% CO2 inlet concentration was maintained by mixing in a mixing chamber. CO2 outlet concentration was also measured by CO2 analyzer (CD 95, Geotechnical instruments, England). 

The catalytic reforming of CH4 by CO2 was carried out in a conventional fixed bed reactor system. Flow rates of reactants were controlled by mass flow controllers [Bronkhorst HI-TEC Co.]. The reactor, with an inner diameter of 0.007 m, was heated in an electric furnace. The reaction temperatoe was controlled by a PID temperature controller and was monitored by a separated thermocouple placed in the catalyst bed. The effluent gases were analyzed by an online GC [Hewlett Packard Co., HP-6890 Series II] equipped with a thermal conductivity detector (TCD) and carbosphere column (0.0032 m O.D. and 2.5 m length, 80/100 meshes), and identified by a GC/MS [Hewlett Packard Co., 5890/5971] equipped with an HP-1 capillary column (0.0002 m O.D. and 50 m length). 

The same samples, after a pretreatment in flowing oxygen (10%) at 625 K, were used as catalysts for the oxidative dehydrogenation of ethanol and methanol in the same reactor. The reaction mixture consisted of O2 (3 or 5%), methanol vapor (3%) or ethanol vapor (5%) and He (balance), all delivered by Tylan mass flow controllers or vaporizer flow controllers. Products were analyzed by gas chromatography. The catalysts exhibited no induction period and their activities were stable over many days and over repeated temperature cycles. 

The catalysts were tested for their CO oxidation activity in an automated microreactor apparatus. The catalysts were tested at space velocities of 7,000 -60,000 hr . A small quantity of catalyst (typically 0.1 - 0.5 g.) was supported on a frit in a quartz microreactor. The composition of the gases to the inlet of the reactor was controlled by mass flow controllers and was CO = 50 ppm, CO2 = 0, or 7,000 ppm, HjO = 40% relative humidity (at 25°C), balance air. These conditions are typical of conditions found in spacecraft cabin atmospheres. The temperature of the catalyst bed was measured with a thermocouple placed half way into the catalyst bed, and controlled using a temperature controller. The inlet and outlet CO/CO2 concentrations were measured by non-dispersive infrared (NDIR) monitors. 

To determine its activity, the catalyst was placed in a quartz microreactor. Reactants were supplied through mass flow controllers and the product composition was determined by mass spectrometry. A typical reaction mixture contained 3.600 ppm NO, 1.06% CH4, and 6.0%... 

P Ij The liquid volume flow to the micro reactor is controlled by an HPLC pump [38]. The gas flow was set by mass flow controllers. Temperature was monitored by resistance thermometers. 

The surface of the micro channels was anodically oxidized to create a pore structure and thereafter wet-chemically impregnated [61]. The liquid reaction solution was fed by an HPLC pump hydrogen was metered by a mass-flow controller. Pressure was kept constant... 

Figure 5.28 Schematic of the experimental set-up. Water/ethylene glycol/SDS reservoir (a) high-pressure liquid pumps (b) catalyst/ substrate HPLC injection valve with 200 pi sample loop (c) hydrogen supply, equipped with mass flow controller (d) micro mixer (e) heating jacket (f) tubular glass or quartz reactor (g) back-pressure regulator (h) [64],...

P 23] Aqueous NaOH solutions of 0.1, 1.0 and 2.0 M were used, fed by pumps to the micro devices [5]. Carbon dioxide was supplied as a mixture with nitrogen, the flow rate being set by a mass-flow controller, liqmd samples were taken and subjected to carbonate analysis (see original citation in [5]). 

P 28/The Hquid feed was introduced by a pump and the gas feed using a mass-flow controller [10], The reaction was carried out using liquid flows of 20.7-51.8 ml h and gas flows of 1.7-173 mlrnin . The gas and liquid velocities amounted to 0.02-1.2 and 0.03-3.0 m s , respectively. The reaction was performed in mixed flow regimes, including bubbly, slug and annular patterns. The specific interfacial areas amoimted to about 5000-15 000 m m . The reaction was conducted at room temperature. 

Two separate 2.1 L reservoirs contain the catalyst and product phases and the contents are fed into the reactor through a standard liquid mass flow controller. The contents of the reactor can be sampled from a pressure fed sample tube. The pressurized liquid reactor products exit the reactor through a pressure control valve, which reduces the pressure to atmospheric, and the liquid contents are delivered to a continuous decanter where the phases separate. The catalyst phase then settles to the bottom where it is drained for recycle and reuse, while the product phase is collected into a 4.2 L reservoir. 

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