INTRODUCTION for THE AIDAN PROJECT
The Aidan project, phase I, requires a small prototype reactor to demonstrate the exponential output of energy for the reaction process.
PRODUCT/PROCESS
Scalability is demonstrated by starting with a small flow of input chemicals with a specific base line of heat generation. The base reaction has predictable heat generation at standard conditions. By changing the input temperatures with inline heating devices, the measurable increase in heat generation can be measured and documented. The entire prototype can be built and operated by a 3rd party independent lab which will verify the patented process and parameters.
GENERAL DESCRIPTION OF PROTOTYPE
The device will be a tubular reactor at 4” diameter about 36” long. The 4” diameter reactor will have a water jacket with 8” diameter allowing a 2” water jacket around the reactor. The 8” jacket will contain a loose spiral turbulator coil allowing flow in the same direction as the reaction products. The reaction chemical inputs will be introduced at one end with the ammonia-steam mix at the 2” point, flooding the reactor for 6”. The acid will be introduced at the 8” point in the center of the annular reactor cross section. The water jacket will attach at the 2” point and end at the 34” point. The 36” reactor byproduct outlet will connect to a cool-down-condenser to reduce the discharge temperature to less than 120F for accumulating the byproducts. All input and output streams will have thermocouple wells stubbed into the streams to read the temperatures.
The input pipe size for “ammonia-steam mix” will be ¾” screwed.
The input pipe size for the sulfuric acid will be ½” screwed.
The input pipe size for the water will be 1.5” screwed.
The outlet pipe size for the 4” tubular reactor will be 1.5” screwed.
The outlet pipe size for the water will be 2” screwed.
For short duration testing only, the reactor will be constructed with Schedule 40, black iron pipe for convenience. Duration testing may establish the longevity of the inexpensive black iron. Future reactors may be constructed with appropriate stainless steel, 416L, or exotic metals such as Zirconium.
Each input stream will have a positive displacement pump which will operate at variable speeds.
Each input stream will have a flow-meter to accurately measure the rate of flow.
There are practical limits to the heat transfer ability of the testing prototype. The 36” tube reactor has 3.1sf of transfer surface and may not be able to transfer enough heat to the cooling water to prevent warping of the reactor. We will discover the practical limits with inexpensive materials.
THE MASS FLOW RATE
The flow rates will produce the generated heat of reaction allowing for a range of testing temperatures.
Using a 6 gpm water jacket stream, baseline 33F rise, the reactor would generate 99,000 btuh.
Using an overflow of ammonia in the steam, the sulfuric acid rate becomes the critical flow measurement. The 99,000 btuh is selected for a 1.0 lb-mole reaction for testing.
The chemical reaction for producing ammonium sulfate is: 2 NH3 + H2SO4 → (NH4)2SO4
The Heat of Reaction, ∆HRXN 25C, based on a standard reaction is calculated from the heats of formation:
-∆Hf NH3 = 28,908 btu/lb-mole
-∆Hf H2SO4 = 349,038 btu/lb-mole
-∆Hf (NH4)2SO4 aq = 504,684 btu/lb-mole
In a 1.0 lb-mole reaction, 34 lbs of NH3 react with 98 lbs of H2SO4 to produce 132 lbs of (NH4)2SO4
∆HRXN 25C for Ammonium Sulfate = (-504,684) – (349,038 + (2 x -28,908)) = -97,830 btu/lb-mole. On this basis we will flow into the reactor at the following rates.
Ammonia: 40 lbs per hour (= 34 lbs plus 18% overflow)
Steam: 40 lbs per hour
Sulfuric Acid: 98 lbs per hour
The attached chart describes the exothermic reaction of ammonia and sulfuric acid under varying input conditions of increasing reactant input temperatures. The reaction is setup by first mixing ammonia with steam in the reactor. The temperature of the steam-ammonia mixture is the governing factor in controlling the exponential exothermic release of the heat of reaction. The following ∆HRXN over the temperature range is read from the data and the chart:
∆HRXN 25C steam = -97,830 btu/lb-mole of (NH4)2SO4 → water rise = 33F
∆HRXN 100C steam = -130,000 btu/lb-mole of (NH4)2SO4 →water rise = 43F
∆HRXN 216C steam = -169,000 btu/lb-mole of (NH4)2SO4 →water rise = 56F
∆HRXN 300C steam= -920,000 btu/lb-mole of (NH4)2SO4 →water rise = 306F
Note: at 300C steam, the water flow will need to be increased to 12 gpm with a rise of 153F
∆HRXN 310C steam = -1,190,000 btu/lb-mole of (NH4)2SO4
Note: at 310C steam, the water flow will need to be increased to 16 gpm with a rise of 149F
∆HRXN 315C steam = -1,398,000 btu/lb-mole of (NH4)2SO4
Note: at 315C steam, the water flow will need to be increased to 19 gpm with a rise of 147F
Assume an inlet water temp of 60F rising 150F to a leaving temperature of 210F as a limiting factor.
THE CHART ABOVE IS THE TARGETED PERFORMANCE CHART FOR THE PROTOYPE HEAT GENERATOR
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