SOLAR CHLORINE PRODUCTION MODULE "SCPM"

Abstract

The Solar powered chlorine producing module, SCPM, is a multi-purpose invention. It is designed to provide daily use of chlorine and caustic soda for water and sewer treatment plants in municipalities throughout the world. This design reduces the operating cost of water and sewer plants in such a way that the initial capital cost will be captured within a few years.

This invention is designed to replace the chlorine producing plants which are expensive to build and costly to operate. They use enormous electric energy taken from already overloaded power grid.

This invention eliminates transporting chlorine, which is considered hazardous material from producing plant to end users' sites. In addition to safety, it also eliminates the liquefaction and transportation cost. Currently, the chlorine end users need storage facilities for hazardous chemicals, which will be eliminated by use of the SCPM system.

Numerous industries use chlorine in daily processing and productions. They could use this system at their own site. Unlike conventional chlorine productions that are built with constant capacity production for their entire life with high initial capital cost, this design is flexible to the chlorine needs of user facilities. A chlorine production plant with solar powered chlorine producing modules is flexible, expandable with minimum initial capital investment that is suitable for any chlorine consumer facility.

Claims

1. The Solar Chlorine Producing Module, SCPM, is an invention by integrating nonrelated existing science fields to develop a commercial producing chlorine unit. This invention brings the science of universities' class rooms to state of productivity in chemical industries. The prime motivations for invention of SCPM are solar power, energy conservation, environmental protection, and lowering overall cost. The SCPM, of claim 1 is designed to produced annually 50 tons of chlorine, 56.5 tons of pure caustic soda, and 1.4 tons of hydrogen. The SCPM, annually will use 125,000 kWh solar power and 83 tons of pure table salt. The importance of SCPM invention can be better realized, when in the list of top fifteen products of chemical industries in U.S. and world, caustic soda ranks number nine, chlorine ranks number 10, and together rank number three. The Solar Chlorine Producing Module, SCPM, of claim 1 is developed as commercial producing chlorine unit with lowest energy used per ton of chlorine, minimum maintenance cost, and low capital cost. SCPM can pay off its initial capital cost in six years with annual return rate of 16.6%.

1. The SCPM of claim 1, in contrast with existing chlorine plants, is independent from power utility networks. It generates the power needs by its Solar Power producer.

2. In solar power producer of SCPM claim 1, the solar irradiation capture is made of N frames, and in this case N is 64 frames that arranged as eight columns of eight frames, making maintenance and troubleshooting easy. Electrically all frames are connected in parallel.

3. Each Solar Frame of power assembly has four commercial solar panels. From wide spectrum of solar panels with different efficiencies and costs, by optimization method, the best in market that generate more power with less cost has been selected. The solar panel in SCPM is Crystalline Silicon Model LG265 SiC 265 G3 with dimension of 65401.4 and efficiency of 16.6%. Panel produces 270 watts AC power, with 31.4 volts and 8.46 Amps. Panel manufacturer is MONOX and it is mass product and stock item.

4. The solar power producer of SCPM claim 1 has out pot of 68 KW DC power with 31.4 volts and 2200 Amps.

5. The chlorine producing unit C12 unit of SCPM of claim 1, is membrane cell that has lowest energy use per ton of chlorine and its solar power source causes less CO2 releases to air and can be accepted as environmental cleaner, while the mercury cell and diaphragm cell are environmental plotters, as they use power from utility networks and release mercury and asbestos to environment.

6. The Cl2 unit is made of M number of cells. The SCPM of claim 1 has nine cells. Electrically connected in series parallel. Cells are PVC slim cylinders with 8 inches in diameter and 60 inches tall to maximize the ion capture area of cathode and minimize the travelling path of ions to reduce the electrolysis energy. A membrane cylinder of 4 inches diameter separate cathode from anode. Each cell operates with 3-3.3 voltage and 2200 Amps. Cells are electrically connected in series, but their product piping lines are connected in parallel.

7. The SCPM of claim 1 is the most economical commercial chlorine producing unit. Its initial capital cost is fraction of conventional units due to elimination of power installation to convert high voltage AC power to very low voltage DC power, as well as elimination of special storage and processes such as purification, liquidation, bottling and transportation.

8. The SCPM of claim 1 as a commercial chlorine producing unit has the lowest annual running cost and maintenance cost, it uses free energy and assembly is simple and trouble free.

9. The SCPM of claim 1 is environmentally friendly, in contrast to existing traditional chlorine facilities. No restriction would be applied by EPA for its site selection and it can be built anywhere.

10. It could be marketed as shelf items.

Description

CDETAILED DESCRIPTION OF INVENTION

[0132] The Invention is Solar Powered Chlorine Producing Module for 50 tons of chlorine per year, called SCPM.

[0133] SCPM has two main parts:

ASolar panel assembly that provides power called solar power producer
B Chlorine Producing Unit called Cl.sub.2 Unit

ASolar Power Producer 215:

[0134] FIG. 9 depicts a SCPM (Solar Powered Chlorine Producing Module) with 50 ton Cl.sub.2 per year.

[0135] The power source of this module is the assembly 215 that is made of 64 solar frames 208, and arranged in eight columns. Each column has eight (8) solar frames 208. The solar frame 208 are made from four (4) commercially silicon solar panels of 209. The solar panel is model LG265 Si.C 265G3 product line of Monox that its specification is already given in the solar section. All sixty-four (64) solar frame are electrically connected in parallel according to wiring 210, and the final power feeder 211 to Cl.sub.2 unit 212 will have voltage of 31 volts and the current of 2233 amps.

[0136] Feeder 211 of FIG. 9 could be a single copper bus strap start from the right-hand side to the left side with the following dimensions: [0137] 1. Section C1C2 and D1D2 will have a cross-section of 2 (10.sup.m/m54.sup.m/m) or 1800 MCM, THHN wire carrying 558 amps [0138] 2. Section C2C3 and D2D3 will have a cross-section of 5.5 (10.sup.m/m75.sup.m/m) or 2800 MCM, THNN wire carrying 1116 amps [0139] 3. Section C3C4 and D3D4 will have a cross-section of 3 (20.sup.m/m80.sup.m/m) or 3800 MCM, THNN wire carrying 1675 amps [0140] 4. Finally, Section C4C5 and D4D5 and throughout of Cl.sub.2 unit will have a cross-section of 4 (20.sup.m/m110.sup.m/m) or 4800 MCM, THNN wire carrying 2233 amps

[0141] Cl.sub.2 Unit 212 Electrical Connection 211:

[0142] FIG. 10 depicts the power supply 211 to Cl.sub.2 unit 212. The Cl.sub.2 unit 212. Has nine (9) membrane cells 214, each operating with 3.3 volts and 2233 amps. Membrane cells are electrically connected in series connection 213.

Specification of Solar Power Assembly 215:

[0143]

TABLE-US-00003 Solar Irradiance 1000 Watts/m2 Solar Panel 209 model LG 265 SIC 265 G3 Manufacturer Monox Solar Panel 209, dimension 165 Cn 100 Cn 3.5 Cn Solar Frame 208 dimension 330 Cn 200 Cn 3.5 Cn No. of Panel 209 in frame 208 2 2 panels (4 panels) Frame 208 Pmax 1082 watts Frame 208 V.sub.Max 31.4 volts Frame 208 I.sub.SC Max 34.9 amps No. of Frame 208 in solar assembly 64 frames Solar power 215 operating voltage 31 volts Solar power 215 operating current 2233 amps Solar power 215 capture area 422 M.sup.2

BChlorine Producing Unit Cl.SUB.2 .Unit 212

[0144] FIGS. 11-A, 11-B and 11-C depict frontal view, side view, and cross-sectional view of new membrane chlorine producing Unit 212 in FIG. 9, that will be used in this invention. FIG. 11-A depicts the arrangement of a row of nine (9) cells 108, piping connection of entering saturated Brine 100 and leaving depleted Brine 116, diluted Caustic 121 and 33% Caustic 113 leaving the Unit. FIG. 11-B depicts the structural Frame 114 to support the two rows of membrane Cells 108, saturated Brine 100 and its branches to Cells 108, diluted Caustic 121, and pure Water 112 and its branches to diluted Caustic 121. FIG. 11-C depicts the cross-section of one cell with its related piping. Brine Container 108 is a PVC slim cylinder, a non-permeable ion-exchanger Membrane 107 divided the Container 108 into Anode Chamber 109 and Cathode Chamber 110. Saturated Brine 100 enters Anode Chamber 109 and depleted Brine 116 leaves the Anode Chamber 109 at the top. Pure Water 112, along with diluted Caustic 121, enters at the bottom of Cathode Chamber 110 and 33% Caustic Soda 113 leaves Cathode Chamber 110 at the top. Chlorine Gas 104 leaves the Anode Chamber 109 at the top, and Hydrogen Gas 105 leaves at the top of Cathode Chamber 110.

Anode 101:

[0145] Up to 1970 electrolytic cell, anodes were graphite. New anodes are Titanium (Ti) metal electro-coated with an Oxide of Platinum group family (Ruthenium, Titanium, Tin and zirconium). Titanium anode Electro-Coated with Ruthenium Oxide (RUO.sub.2) and Titanium oxide (TiO.sub.2) are high current density in low voltage. The use of RUO.sub.2 and TiO.sub.2 coated Titanium Anodes reduces energy consumption by about 10% and higher life expectancy. Competitive design of anode geometry is today's industry challenge, all with the aim of improving gas release, to reduce Ohmic resistance losses and increase the anode life by improving the homogeneity of the brine.

Life of Anode:

[0146] Metal Anode lives are 12, 8 and 4 years for diaphragm, membrane, and mercury, respectively. In mercury cell, short circuit between anode and cathode cause the wear of anode coating.

Cathode 102:

[0147] Is nickel often coated to reduce energy consumption? Reducing the distance between Anode 101 and Cathode 102 will reduce the ohmic resistance and Will reduces the operating voltage and energy. This is the reason behind the new slim cylinder cells.

[0148] Recently, a new oxygen depolarized cathode (ODC) has been used. Oxygen is pumped into the cell to react with liberated hydrogen in Cathode to form water, results in lower cell resistance, and lower the voltage needed for the electrolysis process. This voltage reduction could be as low as 50%. A disadvantage of this process is that the hydrogen is no longer available as an important and valuable product.

Membrane 107:

[0149] Membrane 107 with thickness 0.15 to 0.3 mm is co-polymer of tetra-fluoroethylene (C.sub.2.F.sub.4) Groups, and is non-permeable, but ion exchanger membrane.

Maintenance and Operation:

[0150] To reduce the maintenance cost of cell operation, the following precautions should be considered: [0151] 1Organic acids, Fluorides and Manganese cause damage to anode's Coating. [0152] 2Operation in alkaline brine with PH bigger than eleven (PH>11) will cause a rapid destruction of the Anode's coating [0153] 3Operation with low concentrated and cold brine led to production of Sodium Hippo Chloride (Cl O Na) that should be avoided.

Membrane Cell Consumption and Productions:

[0154] The following numbers are the, products, material and energy used, as base, to produce one metric ton (1000 kg) of chlorine gas: [0155] aOne metric ton of chlorine gas. [0156] bOther Products; [0157] b.sub.11.128 tons of 100% Na OH (Sodium hydroxide). [0158] or b.sub.2Alternatively, 1.577 tons of 100% KOH (Potassium hydroxide). [0159] cBy product of 28 Kg hydrogen. [0160] dRaw material; [0161] d.sub.11.66 tons of pure table salt (Cl Na). [0162] or d.sub.22.1 to 2.2 tons of potassium chloride (Cl K). [0163] eEnergy used; [0164] e.sub.1To-day's Membrane Cells use 2,500 KWH per one metric ton of chlorine. [0165] e.sub.2Extra 500 KWH will used to concentrate the caustic soda to 50%.

Product's Purification and Concentration:

Chlorine Purification;

[0166] Chlorine produced by all cells has some water vapor. Concentrated sulfuric acid (92% to 98% of So.sub.4H2) is used to dry chlorine. If re-concentration takes place at site, also a small amount of the sulfuric acid per ton of chlorine will be used for elimination of (ClONa) and PH control.

[0167] Caustic soda produced by cells has some Cl Na, by boiling the product; excess salt will be crystallized and separate from caustic soda.

Caustic Soda Concentration;

[0168] Indirect heating with steam will do caustic soda concentration, and sulfuric acid concentration.

Specification of Designed Cl.SUB.2 .Unit 212

[0169]

TABLE-US-00004 1 - Unit capacity 50 ton/year 2 - Number of membrane cells nine cells 3 - Power supply: solar a - Operating Voltage V.sub.op a-1 -V.sub.op Max (Noon time) 34 volts a-2 -V.sub.opMin (Morning & Afternoon) 3.4 volts b - Operating current I.sub.op b-1- I.sub.op Max (Noon time) 2233 AMPS b-2 - .sub.Iop Min (Morning & Afternoon) 700 AMPS 4 - Membrane: a - current density design KA/Ft.sup.2 450 AMPs/Ft.sup.2 4.84 Kamp's/M.sup.2 b - Area/cell 5 Ft.sup.2/cell c - Membrane Diameter 4 inches d - Membrane length 60 inches e - Membrane Area/cell actual 5.23 Ft.sup.2/cell f - Current Density actual 426.7 AMPS/Ft.sup.2 4.59 Kamp's/M.sup.2 g - Cl.sub.2 Unit total area (9 5.23 M.sup.2) 47 Ft.sup.2 (4.37 M.sup.2) 5 - Production per year: a - Chlorine gas (metric ton = 1000 Kg) 50 ton/year b - Caustic Soda 100% 56.4 ton/year 50% 112.8 ton/year c - Hydrogen 1.4 ton/year

Case Study:

[0170] This invention was applied in design of chlorine producing plant for a municipality with a population of 170,000.

[0171] In this design, the production capacity could be increased throughout the life of the plant if chlorine demand increases. In the 25-year life of the plant, there will be four times capacity expansion at the start of the 2.sup.nd, 3.sup.rd, 4.sup.th and 5.sup.th period of five years period with addition of 3, 3, 4, and 3 SCPM, 50 ton/yr. to the plant. Due to this expansion, the increase of Cl.sub.2 production takes place in four (4) steps, while the city demand is exponential; that results in excess Cl.sub.2 production.

[0172] The excess chlorine will be sold to other cities at 80% of the buying price of offsite Chlorine by city, as an income to the city.

[0173] The city's caustic soda consumption is about 33% of the plant production. The 67% excess product of the plant will be sold to other cities at 75% of the buying price of offsite caustic soda by city, as an income to the city.

[0174] The plant hydrogen by-product may be sold at the price of 75% of the market price as income to the city.

[0175] If, instead of selling the hydrogen, it is converted to ammonia (NH.sub.3), it will provide 56.5% of City's consumption, and the city needs to buy only 43.5% of its consumption.

[0176] The summary of this case study has been given in the following graphs. [0177] FIG. 12depicts the City's population from 2008 to 2040 according to the U.S. Census Bureau [0178] FIG. 13depicts the City's chlorine (2015-2040): [0179] a. Annual chlorine consumption [0180] b. Annual suggested plant production [0181] FIG. 14depicts the City's caustic soda (2015-2040): [0182] a. Annual caustic soda (Na OH) consumption [0183] b. Annual suggested plant production [0184] FIG. 15depicts the City's ammonia (2015-2040): [0185] a, Annual ammonia NH.sub.3 consumption. [0186] b, Annual ammonia NH.sub.3 production [0187] FIG. 16depicts: The city's cost for chlorine and caustic (2015-2040): [0188] a. Annual cost of chlorine consumed [0189] b. Annual cost of caustic soda consumed [0190] c. Total City's annual cost of Cl.sub.2 plus caustic soda. [0191] FIG. 17depicts the initial required number of SCPM modules in the plant, and the number of SCPM modules in the plant's expansion to meet the City's chlorine demand. [0192] FIG. 18depicts the City's hydrogen (H.sub.2) product as the plant's by-Product. [0193] FIG. 19depicts: [0194] a. City's income by selling hydrogen at 75% of market price. [0195] b. City's income if all hydrogen converted to ammonia (NH.sub.3) as supply near of 57% of City's ammonia consumption. [0196] FIG. 20depicts: [0197] a. The cost of solar power 215 per module SCPM, FIG. 9. [0198] b. The cost of Cl.sub.2 unit 212 per module SCPM, FIG. 9. [0199] FIG. 21depicts: [0200] Accumulated plant capital cost in 25 years period. [0201] FIG. 22depicts the plant's total running cost in 25 years. [0202] FIG. 23depicts [0203] a, Employees wage to operate the plan through its life span of 25 years. [0204] b, the cost of annual Table Salt consumed as raw material for 25 years plant's life span. [0205] FIG. 24 depicts [0206] a, plant's total income per 5-years period. [0207] b, Accumulated plants total cost in 25 years. [0208] c, Accumulated plants total income in 25 years. [0209] At year 2040 (the end of plant's life) [0210] the total accumulated income in 25 years is about $76,300,000. [0211] the total accumulated cost including capital investment and running cost (Running energy+Maintenance+Replacement) in 25 years is About $33,560,000. [0212] The plant's net income in 25 years is $42,740,000.

BRIEF DESCRIPTION OF DRAWINGS

[0213] To explain and better understanding of drawings, assigned numbers has identified the products, elements of solar power producing unit, chlorine producing cell assembly, and related accessories. The assigned numbers used in figures are given in the following table.

DESCRIPTION OF ASSIGNED NUMBERS

[0214]

TABLE-US-00005 ASSIGNED ITEM DESCRIPTION NUMBERS 1 Electrolyte Solution: 100 Acid + Water/Salt + Water 2 Anode 101 3 Cathode 102 4 DC Power Source 103 5 Anion (Non-metallic elements) 104 Cl.sub.2, O.sub.2 6 Cation (Metallic elements) Na, Fe, H 105 7 Caustic Soda under 30% 106 8 Diaphragm or Membrane 107 9 Cell Container 108 10 Anode Chamber 109 11 Cathode Chamber 110 12 Diluted Brine 111 13 Pure Water 112 14 Caustic Soda 33% 113 15 Structural Frame 114 16 Brine Concentrator 115 17 Depleted Brine 116 18 Decomposer 117 19 Amalgam (Na Hg) 118 20 Recycled Mercury 119 21 Caustic Filter 120 22 Diluted Caustic Soda 121 23 Solar Panel at 32 200 24 Solar Panel at Noon 201 25 Solar Panel at 6:00 a.m. & 6:00 p.m. 202 26 Sun at 6:00 a.m. & 6:00 p.m. 203 27 Sun at Noon 204 28 Sunlight at Noon 205 29 Sunlight at 6:00 a.m. & 6:00 p.m. 206 30 Horizon 207 31 Solar Frame 208 32 Solar Panel 209 33 Parallel Connection 210 34 Power to Cl.sub.2 Producing Unit 211 35 Cl.sub.2 Producing Assembly Unit 212 36 Series Connection 213 37 SCPM Membrane Cl.sub.2 Cell 214 38 Solar Power Producing Unit Assembly 215

[0215] FIG. 1 shows the basic set-up in the laboratory. It explains electrolysis of water with hydrochloric water 100 or solution of Table Salt 100 into their elements. Water 100 breaks down into Oxygen 104 in Anode 101 and Hydrogen 105 in Cathode 102. Table sale Solution 100 breaks down into Chlorine 104 in Anode 101 and Na OH 106 in Cathode 102.

[0216] FIG. 2 explains the concept of diaphragm cell for producing chlorine from saturated table salt solution. Diaphragm 107 divides Container 108 into two sections of Anode Chamber 109 and Cathode Chamber 110. Saturated Brine 100 enters Anode Chamber 109 at the top. Chlorine ions will be attracted to anode 101, give up one electron, and become chlorine Gas 104 that accumulates at the top of Anode Chamber 109. Sodium ions pass through Diaphragm 107 and enter Cathode Chamber 110. Some interact with Hydroxide Ions (OH.sup.1) from Cathode 102 to form Caustic Soda 106, while some attract to Cathode 102, receive one electron and convert to metallic sodium. Metallic sodium reacts with water to produce Caustic Soda 106 and Hydrogen 105 which accumulates at the top of Cathode Chamber 110.

[0217] FIG. 3, is a view of commercial diaphragm cell. In this Figure, Brine 100, Anode 101, Cathode 102, Power 103, Chlorine Gas 104, Hydrogen Gas 105, diluted Caustic Soda 106, Diaphragm 107, Container 108, Anode Chamber 109, Cathode Chamber 110, Diluted Brine 111, and 30% Caustic Soda 113 are given. Diluted Brine 111 passes through diaphragm 107 into Cathode Chamber 110.

[0218] FIG. 4, is a simplified view of a membrane chlorine producing cell. A non-permeable and ion-exchanger membrane 107 divides the Container 108 into two Anodes, Chamber 109 and Cathode Chamber 110. Saturated Brine 100 enters from the bottom to Anode Chamber 109 and as depleted brine 116 leaves the Chamber 109 at the top. Caustic Soda 106 and Water 112 enter the Cathode Chamber 110 at the bottom and as it moves up, it picks Caustic Soda generated in Cathode 102. Rich Caustic Soda 113 with 30% to 33% density leaves at the top. Chlorine Gas 104 accumulates at the top of Anode 101 and Hydrogen Gas 105 collects at the top of Cathode 102.

[0219] FIG. 5, shows a view of commercial chlorine membrane cell. All elements in this drawing is the same as FIG. 4 except that the brine circuit from saturated 100% entering the Anode Chamber 109, loses its chlorine ions to Anode and becomes depleted Brine 116 that enters into concentrator 115, becomes saturated Brine 100 and repeats the cycle. Caustic Soda 33% of 113 enters to caustic container and leaves the cell. Caustic soda 106 as Part of Caustic Soda 113 becomes diluted with Water 112, enters to Cathode Chamber 110, receives caustic from Cathode 102 and becomes 33% Caustic 113. Ions of Na.sup.+1 Enter Cathode Chamber 110, some interact with Hydroxide ions (OH.sup.1) from Cathode 102 to from Caustic Soda 106, and some attract to Cathode 102, receive one electron and convert to metallic Sodium. Metallic Sodium reacts with water to produce caustic soda 106 and Hydrogen 105, which accumulates at the top of Cathode Chamber 110.

[0220] FIG. 6, shows a simplified view of Chlorine Mercury Cell. A mercury film over an inclined flat surface acts as Cathode 102. Anode 101 is metal plates parallel to mercury surface and in close distance. Saturated Brine 100 enters the Container 108 from the top. It gives away its chlorine ions to Anodes 101 that become Chlorine Gas 104. Its sodium ions go to mercury Cathode 102 and by receiving one electron become Metallic Sodium. Sodium reacts with mercury and forms Amalgam (NaHg 118) that leaves Cathode 102. After all this process, saturated Brine 100 becomes depleted Brine 116 that leaves the cell at the top. Amalgam (NaHg 118) in Decomposer 117 reacts with Water 112, breaks down into Caustic Soda 50% 113 and Hydrogen 105 and recycled Mercury 119. Hydrogen 105 will be collected at the top of the Decomposer 117 and Mercury 119 will be pumped to Cathode 102.

[0221] FIG. 7, Shows a view of commercial mercury chlorine cell. All elements and process are identical to FIG. 6.

[0222] FIG. 8, Shows a rotating solar Panel 200. Panel orientation at Noon 201 has a tilted angle of 42, and panel Position 202 has better efficiency at early morning and afternoon. The sun's location is given at Noon 204 and for early morning and late Afternoon 203, having angles of 42 and 32 respectively with horizon 207

[0223] FIG. 9, Shows Solar Power Producer 215, part of invention of SCPM (Solar Powered Chlorine Producing Module). Solar power Producer 215 is made of eight columns and each column has eight Frames (208), with the sixty-four (64) frames. Each Frame 208 has four solar panels of 209. In this assembly, all panels are connected electrically in Parallel 210 and the power to chlorine cells 211 has 30 v and 2233 amps.

[0224] FIG. 10, Shows Membrane Cells 214 is electrically connected in Series 213. Power feeds to Assembly 211 has 30 v and 2233 amps.

[0225] FIG. 11-A, Shows front view of SCPM-Chlorine Producing Cell assembly and its associated piping. The Assembly has nine (9) membranes Cells 108. The cell's detail is given in FIG. 11(c). Saturated Brine 100 enters Anode Chamber 109 cells from the bottom strip off its ions, moves up and leaves the cell as depleted Brine 116. Diluted Caustic Soda 121 mixes with pure Water 112 and enters at the bottom of Cathode Chamber 110. As it moves up, it receives Caustic Soda (Na OH) from Cathode 102, becomes rich Caustic 113 with 33% that leaves the Assembly at the top.

[0226] FIG. 11-B, Shows the side view of SCPM-Solar Chlorine Producing Module. The view shows two membrane Cells 108 and associated piping. The main saturated Brine 100 and its branch feed to each cell located at the bottom. Diluted Caustic Soda 121 and pure Water 112 and their associated piping are located at the bottom of the cell. Structural metal Frame 114 supports cells and associated pipes. Caustic Soda 33% collector Pipe 113 and its branches to cell's cathode chamber are located at the top. Hydrogen collector Pipe 105 and its branches to cathode chamber are located at the top of the cell. Depleted brine collector pipe 116 and chlorine collector Pipe 104 and their branches to cell's anode camber are located at the top of the Assembly.

[0227] FIG. 11-C: Shows the cross section of membrane cell. Brine Container 108 is divided by cylindrical non-permeable and ion exchanger Membrane 107 into Anode Chamber 109 and Cathode Chamber 110. Saturated Brine 100 enters Anode Chamber 109 at the bottom, gives up its ions as it moves up and becomes depleted Brine 116 that leaves the cell a t the top. Chlorine Gas 104 releases from Anode 101, will be collected at the top of Anode Chamber 109, and leaves the cell. Diluted Caustic 121 mixes with pure Water 112 and enters Cathode Chamber 110 at the bottom. As it moves, up, it absorbs caustic soda from Cathode 102 and becomes Caustic Soda 113 with 33% that leaves the cell at the top. Hydrogen Gas 105 that release from Cathode 102 will be collected at the top of Cathode Chamber 110 and leaves the cell.

Case Study's Figures

[0228] FIG. 12, The City's population from Year 2000 to Year 2040

[0229] FIG. 13, The City's chlorine consumption (2000-2040) and chlorine produced by SCPM Plant from Year 2015 to 2040

[0230] FIG. 14, The City's caustic soda (Na OH) consumption and caustic soda produced by SCPM plant from year 2015 to 2040

[0231] FIG. 15, The City's ammonia (NH.sub.3) consumption and SCPM ammonia production from Year 2015 to 2040.

[0232] FIG. 16, The City's cost for used chlorine (Cl.sub.2) and caustic soda (Na OH) and their total from year 2015 to 2040

[0233] FIG. 17, The City's plant required number of SCPM (module with 50-ton chlorine Production per year) from Year 2015 to 2040.

[0234] FIG. 18, The City's hydrogen production, by city chlorine plant from Year 2015 to 2040.

[0235] FIG. 19, The City's income if hydrogen is marketed directly, or converted to ammonia From Year 2015 to 2040.

[0236] FIG. 20, The cost of one solar power assembly 215, (FIG. 9) and one chlorine cell assembly 212, (FIG. 9) of one SCPM from Year 2015 to 2040.

[0237] FIG. 21, The City's initial capital cost in Year 2015 and additional capital cost for the Plant's capacity increase for four periods of five years, from 2015 to 2040.

[0238] FIG. 22, The Plant's total running cost from Year 2015 to 2040, and two major chlorine cells replacement in Years 2025 and 2035.

[0239] FIG. 23, The City's chlorine plant cost of raw material and labor, [0240] athe plant's cost of employees that run the plant from Year 2015 to 2040. [0241] bthe plant's cost of used table salt from Year 2015 to 2040.

[0242] FIG. 24, Shows the, capital cost, running cost, and income from 2015 to 2040. [0243] aplant's total gross income per five-year period for 2015 to 2040 [0244] bplant's accumulated cost (capital and running cost) from Year 2015 to 2040. [0245] cplant's accumulated gross income from Year 2015 to 2040 [0246] dShaded area is accumulated net income at any time of plant's life. At 2040 (end life), the accumulated net income well be $42,740,000.At end of the plant's life.