Classifications

• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
  • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
  • C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
  • C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
  • C01B3/08—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents with metals
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/0006—Controlling or regulating processes
  • B01J19/002—Avoiding undesirable reactions or side-effects, e.g. avoiding explosions, or improving the yield by suppressing side-reactions
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/0053—Details of the reactor
  • B01J19/0066—Stirrers
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J7/00—Apparatus for generating gases
  • B01J7/02—Apparatus for generating gases by wet methods
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
  • C01D3/00—Halides of sodium, potassium or alkali metals in general
  • C01D3/04—Chlorides
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
  • C01D3/00—Halides of sodium, potassium or alkali metals in general
  • C01D3/14—Purification
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
  • C01D3/00—Halides of sodium, potassium or alkali metals in general
  • C01D3/14—Purification
  • C01D3/16—Purification by precipitation or adsorption
• • C—CHEMISTRY; METALLURGY
  • C01—INORGANIC CHEMISTRY
  • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
  • C01F7/00—Compounds of aluminium
  • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
  • C01F7/42—Preparation of aluminium oxide or hydroxide from metallic aluminium, e.g. by oxidation
  • C01F7/428—Preparation of aluminium oxide or hydroxide from metallic aluminium, e.g. by oxidation by oxidation in an aqueous solution
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00002—Chemical plants
  • B01J2219/00004—Scale aspects
  • B01J2219/00006—Large-scale industrial plants
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
  • B01J2219/00094—Jackets
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00162—Controlling or regulating processes controlling the pressure
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00245—Avoiding undesirable reactions or side-effects
  • B01J2219/00259—Preventing runaway of the chemical reaction
  • B01J2219/00263—Preventing explosion of the chemical mixture
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00245—Avoiding undesirable reactions or side-effects
  • B01J2219/0027—Pressure relief
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
  • Y02E60/00—Enabling technologies; Technologies with a potential or indirect contribution to GHG emissions mitigation
  • Y02E60/30—Hydrogen technology
  • Y02E60/36—Hydrogen production from non-carbon containing sources, e.g. by water electrolysis

Definitions

• This invention relates to a method of industrial production of hydrogen and other products from waste aluminium and devices for the method.
• waste material in this case aluminium, (aluminium packaging, lids, tubes, closures, beverage cans etc.) is a global issue.
• Hydrogen production from, the reaction of ⁇ luntimurn. with water using .sodium hydroxide as, a catalyst is generally known.
• the products of the reaction are A1 2 0 3 or Al(OH 3 ) and heat.
• Waste aluminium can be used favourably for production.
• the patent file CN 183 6773 introduces a catalyst applied to aluminium waste to remove the protective layer on the surface of aluminium for an improved reaction of aluminium with water.
• the catalyst is a compound containing PVA, ethanol, acetone, mercury chlorides and water.
• aluminium is used in particular as well as alloys of alkali, metals, aluminium, alloys, magnesium alloys, lithium alloys, etc.
• the raw material (fuel) is in the form of dust, powder, compressed boards or cell cartridges.
• Patent file US 6506 360 describes a small compact device for hydrogen production by which the fuel (ground waste aluminium) is fed to a reactor in a fuel cell where it reacts with water in the presence of NaOH as a catalyst with hydrogen and heat production. The intensity of the reaction is controlled by immersion of the fuel cell to avoid overheating of the reactor. The generated heat is not used in any way, and the hydrogen is combusted in a burner.
• the device may be used e.g. as a cooker, it is not suitable for hydrogen production at an industrial level. For hydrogen production at' an industrial level, the device described in patent file DE 340 1194 is used.
• Production takes place in a reactor in the form of a reaction of aluminium in the presence of NaOH as a catalyst with heat, hydrogen and DC current being generated while natrium-aluminate is generated as a by-product.
• Aluminium raw material is placed on a mesh in the reactor; NaOH and water are fed to the reactor through a central funnel then rises above the mesh where it reacts with aluminium.
• the hydrogen is removed and a DC electric current is taken from the electrode arranged inside the reactor.
• a method for the use of heat is not described in detail, but the reactor shell is fitted with a water heat exchanger used for the heating of water and cooling of the reactor at the same time. Natrium- aluminiate is described here as a.
• the task of the invention is to establish a method and device fpr, the production of hydrogen and other products from waste aluminium which, would remove .all the issues described above, which would be safe as well as suitable for the production , of hydrogen at industrial levels, environmentally- friendly (waste-free), and economically effective.
• the objective as specified above is achieved by the method of the production of hydrogen and other products in a reactor by the reaction of aluminium with water in the presence of sodium hydroxide; or potassium hydroxide as a catalyst, according to the presented invention, the basis of which is that the reactor, and/or other accessory devices are depressurized to a negative pressure at least 0.5 kPa with a vacuum pump before the reaction, the reactor is then filled with hydrogen of a minimum purity of 99.8%, the gas is pumped away again with a subsequent filling with hydrogen of a minimum purity of 99.5% again to positive pressure at least 0.1 MPa, whereas the gas removed from the reactor and/or accessory equipment using the vacuum pump is exhausted to, . a . chimney and dispersed into the atmosphere.
• the underlying idea of the invention is the increased safety of hydrogen production in which a safe level must be achieved by exhausting all air from the production device before production, when the oxygen content in the finished hydrogen does not exceed 10 ppm.
• the produced hydrogen is further purified so that the hydrogen produced in the reactor is washed in washing tank in treated service deaerated water and saturated with hydrogen.
• the hydrogen is fed to the washing tank through small holes to aerate in the water column.
• Ferromagnetic admixtures are separated from the reaction liquid, being the mixture of water, NaOH, and aluminium particles, with the use of a solenoid in the tank, the liquid is then fed to the input of a mechanical filter where the mechanical admixtures are separated, then the liquid is fed to the. input of the first 'precipitator of Al(OH) 3j where aluminium hydroxide is precipitated wkh the use of hydrochloric acid and the suspension thus
• the steps towards the final, purification of ⁇ sodium; hydroxide and, separation of salt solution are performed and , the salt solution will. be. used for the next applicable product sodium chloride, so that aluminium hydroxide from the second filter Al(OH) 3 mixes with water in the, washing tank Al(OH) 3 and NaCl contained, in the suspension is dissolved, the suspension is then deposited, the salt solution is fed t the third Al(OH)3 filter;, the tank is filled with water again and the sediment is mixed after analysis in the presence : of I TaCl; the washing process then either repeats or the suspension is fed to the third Al(OH) 3 filter. ,
• hot water be used for operation of the device from the water heat exchanger of the reactor, which is fed to the hot service water tank, from which hot service water is fed to the hot service water tank, from which hot service water is distributed to the second Al(OH)3 precipitator, NaCl crystallizing device and NaCl dryer.
• the inner space,;pf the reactor, low-pressure hydrogen tank and service tank is connected to a vacuum pump and its output is fed to a chimney while at the same time, the feactor, the hydrogen tank and, service tank are independently connected to the chimney via safety valves.
• Connection with, the vacuum pump is used for rinsing the tanks and pumping gas away, a direct connection with the chimney via the safety valves is a safety measure for the case of unexpected and dangerous overpressure in the reactor or another accessory device.
• the issue of service hydrogen required for rinsing of the device is addressed so that the low-pressure hydrogen tank is connected to the medium-pressure service hydrogen tank via the medium- pressure compressor for washing of the reactor and operation tanks for production and treatment of hydrogen and other products for treatment of the; reaction liquid.
• the low- pressure hydrogen tank is connected to high-pressure hydrogen tank via high-pressure compressor from which the compressed'hydrogen is fed to the filling and distributing point of hydrogen.
• Hydrogen can be distributed e.g. in pressure cylinders or otherwise as requested by customer.
• Another of potentially possible method of use of hydrogen produced and treated in this way is re-compressing and use for combustion engine in mixture with oxygen, whereas the combustion engine may drive an alternator or a generator for production of electricity sold to the distribution grid.
• the clean reaction liquid is furthermore reprocessed for reuse, whereas the output of the cleaft reaction . liquid is connected from the inter-tank of the reaction liquid to the input, of reprocessed reaction, liquid tank, whereas the tank is connected with the first tank of sodium hydroxide and the output pf the reprocessed reaction liquid is fed back to the reactor input from the tank,, .. . . , ,
• the device according to the' invention includes a reservoir for cooling water, which is connected with hot water heat exchanger, with washing tank and deaeration and saturation tank.
• ⁇ '" ⁇ ' ⁇ " ⁇ ⁇ the device is modified for the final purification and sale of pure aluminium hydroxide so that output of the reaction liquid from the inter-tank of the reaction liquid; and reprocessed reaction liquid from the tank of the reprocessed reaction liquid is fed to the neutralizing unit connected with the second hydrochloric acid tank and output of the neutralized suspension from the neutralizing unit is fed to input of the first Al(OH);.
• sodium chloride as the final product for sale is prepared.
• Solution of sodium chloride from the first Al(OH).3 filter is fed to the NaCl crystallizing unit from which the crystallized sodium chloride transferred to NaCl store for dispatch via the NaCl dryer.
• the NaCl crystallizing unit is formed at least from one bath with hot service water feed from hot service water tank, fitted with skirrimer of salt steams terminated in a condenser.
• the main input raw material for . hydrogen production is waste aluminium, e.g. bottle caps, lids from yoghurts, pastes and similar products, tubes from condensed milk, packaging from chocolates, butter etc., beverage cans, cream jars, packaging of cheeses and much more.
• This waste material is collected in collection and gathering place 43 of aluminium located outside so-called hydrogen zone, i.e. the zone of the main production equipment where aluminium is produced. From there, aluminium; is transported to sorting , and crushing line 40 also located outside the hydrogen zone.
• aluminium is manuall checked to remove plastic materials, paper etc.
• This sorted waste is transported to an incinerator. Aluminium is then crushed into 4 - 6 mm particles and stored iri. crushed aluminium storage 4J_ that may be located outside the hydrogen zone as well.
• crushed aluminium is transported to filling and dosing device 7, which is already located in the hydrogen zone, and its bin and other components are air-displaced before each operation as any other device in the hydrogen zone.
• the bin of the filling and dosing device 7 is filled with belt conveyor; filling of .crushed aluminium to the reactor I is automatic using a screw-dosing conxeyor.
• Another raw material for hydrogen production is water. Water is pumped from the water pipeline, goes through the water treatment plant 44 and collects in the reservoir 23 of the cooling water located outside the hydrogen zone, from where it is fed primarily to the reactor 1 as well as other parts of the device as described later.
• the next raw material for hydrogen production is sodium hydroxide purchased and stored in the first bin 20 of sodium hydroxide in hydrogen zone from which it is fed to the tank J_9 for reprocessing of the reaction liquid (mixture of sodium hydroxide and water) and then to the reactor I .
• Sodium hydroxide is stored also in the second bin 37 of sodium hydroxide outside the hydrogen zone;'
• the last raw material required 1 for hydrogen production according to the invention is hydrochloric acid collected in the first reservoir 15 of hydrochloric acid in the hydrogen zone and in the second reservoir 36 of hydrochloric acid outside the hydrogen zone and it is used for Al(OH) 3 precipitation and neutralization of the reaction liquid.
• the hydrogen production occurs in the hydrogen zone depicted on figure 1 as the area delimited with dashed line and includes all important devices used for production of hydrogen, particularly the reactor I ,
• the reactor is a closed container in which known chemical reaction for hydrogen production occurs:
• Hydrogen generated in the reactor 1 is removed for washing in the washing tank 6 and the reaction liquid (mixture of H 2 0 and NaOH with aluminium residues) is removed for separation of metal particles to the tank with solenoid 1_1.
• the reaction 'must be 1 mterrupted immediately 'by feeding of cold Hvafdr 1 firbitf the 1 reservoir ⁇ ! f '- ⁇ ⁇ emergency and service'- wafer' and charge of more aluminium frtirri the fil ' lirtg and dbs ri ! line '7 is stopped.
• the reactor 1 is designed ' to negative pressure at ; least 0,5 kPa and positive pressure- 1 MPa. ' ⁇ ⁇ - : - - ⁇ ; r : : 1 " - ⁇ ⁇ 1 ' - ' ' ⁇ il nrA ; .
• the reactor I as well as filling " ancl dosing line 7 ⁇ as well as all other devices in so- called hydrogen zone are interconnected with the vacuum pump 4 so that ihpiuts from each device are fed to the collection pipeline VP.
• the vacuum pump 4 With the use of the vacuum pump 4 the production line must be successively (tank by tank) air-displaced to negative pressure; about 1.3 kPa and subsequently filled with pure hydrogen of at least #9.5% purity before.each time the production line is started or after opening of a tank during operation. This is hydrogen identified as "H 2 rinse” taken from medium-pressure reseryoir 24 of the service hydrogen and distributed to each reservoir in the hydrogen zone.
• each reservoir in the hydrogen, zone is air-displaced again and filled with "H 2 rinse” hydrogen to positive pressure of 0, 1 MPa. All exhausted air as well as rinse hydrogen is taken to the chimney 5 to which the output from the vacuum pump 4 terminates. This process is necessary for safety reasons; exhausting of all air must provide oxygen contents in finished produced hydrogen under 10 ppm.
• the chimney 5 consists of tube of inner diameter , of 150 mm and height over the highest point of the technological device of the production line including roof.
• the chimney 5 is not and must not be fitted with terminal burner.
• Fed mixture of hydrogen and air is exhausted to atmosphere, whereas released hydrogen rises upright and therefore may not accumulate to a phase of explosive mixture, i.e. 1 - 99 % H/0 2 .
• Exhausted hydrogen is not a substance causing greenhouse effect, is neither poisonous nor toxic and not explosive if diluted to high proportion. Environment is not exposed to smell, airborne particles etc.
• Direct output from the reactor 1 is fed to the chimney 5 through the safety valve (used for relieving of dangerous overpressure) and the collection pipeline K of the chimney 5 has terminated outputs from each device and tank in the hydrogen zone fitted with safety valves and they are used for exhaust of dangerous positive pressure.
• An important feature of the production process according to the invention is purification of the generated hydrogen.
• Hydrogen from the reactor I is fed to the washing tank 6. which is 70% filled with treated oxygen-free from the reservoir 13 of the emergency and service water. The remaining 30% of the volume of the washing tank 6 consists of washed hydrogen.
• Hydrogen is fed to the washing tank 6 through small holes to bubble across the water column. In this way, water steam as well as lye drops are removed.
• Water is added to the washing tank 6 from the reservoir 13. of emergency and service water. Certain part of the water used goes to the first precipitator 16 A1(QH) 3 .
• the washed hydrogen goes to separation of water to the separation, tank 8.
• the separation tank 8 is the tank 90% filled with Raschig rings where water from the washing tank 6 is precipitated and -ran down on the rings with subsequent draining to the reservoir 13 of the emergency and service water. Relativel dry hydrogen continues to low- pressure hydrogen tank 3.
• the low-pressure hydrogen tank 3 serves as temporary store for generated hydrogen and for separation of residual water with the use of freezing lamellas cooled down to temperature of - 20 °C. Freezing takes place with the use of the cooler 22.
• the lamellas must be defrosted regularly with the service water from the reservoir 35 of hot service water. Defrosted water is drained to the reservoir 13 of emergency and service water.
• Dried hydrogen is pumped from the low-pressure hydrogen tank 3; with the use of medium-pressure compressor 2 to the medium-pressure reservoir 24 of service hydrogen from where it is used as H 2 rinse for rinsing (filling and air-displacing) of the reservoirs in the hydrogen zone.
• Pressure in low-pressure hydrogen tank 3 must be lower than operating pressure. Water contents in the finished hydrogen should riot exceed 5 ppm.
• Excessive hydrogen from the low-pressure hydrogen tank 3 is fed via high-pressure compressor 21 to high-pressure hydrogen tank 9 where it is stored under pressure of 230 at. Hydrogen is distributed from the high-pressure hydrogen tank 9 in the filling and distributing point 10 of hydrogen.
• the high-pressure hydrogen tank 9 is also fitted with draining 6f residual condensed water drained to the reservoir 13 of the emergency and service water.
• the filling and distributing point 10 of the hydrogen may pose various methods of use and sale of purified product (depends on agreement with customers).
• hydrogen may be filled in pressure cylinders or after repeated pressure reduction it may be used for electricity production when hydrogen is fed to the engine 45 ' that drives the alternator 46 producing electric energy.
• reaction liquid is drained to the tank ⁇ . with solenoid that traps all particles that can be captured by magnet. It may particularly include iron with admixture of trace elements of other metals.
• Reaction liquid flows to the mechanical filter 12, which is the tank fitted with filters arranged in descending order frorn 1 ,000 ⁇ micrometres to 4 micrometres. This filtration removes all mechanical particles larger than; 4 micrometres.
• Pur-ified reaction liquid flows for processing in the first 16 Al(OH)3 precipitator.
• accessory reservoirs are important, particularly the reservoir 13 of emergency and service water mainly used as reservoir of the emergency water for uncontrolled, reaction of the reactor 1. It is furthermore used as reservoir for collection of all service treated and oxygen-free water as well as for preparation of the reprocessed reaction liquid.
• the reservoir 1_3 of the emergency and operation water is connected to the deaeration and saturation reservoir 14 used for deaeration of newly feeding treated water from the reservoir 23 of the cooling water and to subsequent saturation with service hydrogen (H 2 rinse). Water treated in this way is pumped to the reservoir 13 of emergency and service water with the use of the medium-pressure service hydrogen (1 1 2 rinse).
• Another accessory tank is the first reservoir 15. of hydrochloric acid, which is the tank for deaerated HC1 used partially for neutralization of the reaction liquid . in the first J_6 Al(OH) 3 precipitator.
• the suspension is then
• neutralizing unit 25 where full neutralization is performed.
• the reservoir 19 for reprocessing of the reaction .liquid is used for preparation of the reprocessed reaction liquid for further, use in the reactor i.
• 80% of partially neutralized reaction liquid from the inter-reservoir , 18 of the reaction liquid is combined with 20% of new lye from the first reservoir 20 of sodium hydroxide.
• The: reaction liquid treated in this way flows back to the reactor 1 remaining 20% of the reaction liquid flows to the neutralizing unit 25.
• the first reservoir 20 of sodium hydroxide is the reservoir for clean new 50% sodium hydroxide added to the reaction liquid with 20% vol. ; share.
• the lye is deaerated, saturated with hydrogen and it is added to the reservoir 9 for regeneration of the reaction liquid.
• zone without hydrogen is important for operation of the device according to the invention (depicted on figure 1 outside the hydrogen zone with dashed line).
• the first device in the zone without hydrogen is the reservoir of cooling water 23, which is a tank used as reservoir of cooling water for reactor as well as reservoir of treated service water.
• Water for the reservoir 23 is obtained from the water treatment plant 44 from water pipeline or from other source, then also from the recrystallizing unit 27 for NaCl or condensate is fed from the condenser 28.
• Water from the reservoir 23 of cooling water is fed to the reactor 1 , washing tank 6, deaeration and saturation reservoir 14, to the neutralizing unit 25 and to the reservoir 3_1 for washing of Al(OH) 3 as mentioned below.
• Vast majority of the devices arranged in the zone without hydrogen is used for purification of aluminium hydroxide and for refining of its properties for subsequent sale; in addition this device is used for production of sodium chloride and distribution of hot service water.
• the reaction liquid flowing from the inter-reservoir J_8 in the hydrogen zone is fed to the neutralizing unit 25 in the zone without hydrogen.
• condenser 28 cooled service water is drained to the "reservoir' of cooling water 23.
• the condenser 28 serves id condensation of water steams coming from the NaCl crystallizing linit 27.
• Condensed water is drained from the condenser 28 to the reservoir of cooling; afer 23. ' ⁇ '.-Vr
• NaCl dryer 34. the crystallized sodium chloride from the cry stallizin ⁇ unit 27, . is dried in the tubs, also , with the use of hot service water from , the reservoir 35 of that service water, and subsequently it is manually .transferred to NaCl store 38 NaCl for dispatch. Salt steams from, drying are drained to atmosphere. ⁇ ..;
• the second precipitator 29 A1(0H) 3 is a tank where aluminium hydroxide is from the filter 17 for removal of A1(0H) 3 in the hydrogen zone and from the first filter 26 Al(OH) in the zone without hydrogen
• the second filter 30 is also fitted with the filters of descending mesh size from 80 micrometres to 20 micrometres.
• the precipitated hydroxide is separated and then manually transferred to the reservoir 31 for washing of Al(OH) 3.
• Liquor is pumped for hydrogen treatment to the reservoir 42 for deaeration and saturation and lye saturation with hydrogen in the hydrogen zone.
• the filtered hydroxide from the second filter 30 is mixed with clean water from the reservoir of cooling water 23 and NaCl present in the suspension is dissolved under constant stirring. Then the suspension is let to sediment, flow off drains the salt solution to the third filter 32 Al(OH) 3j clean water is filled again and the sediment is mixed after NaCl presence analysis.
• the suspension is drained to the third filter 32 Al(OH) 3 .
• the third filter 32 6f aluminium hydroxide consists of the tank fitted with filters of 80 micrometres to 20 micrometres in descending order. In this tank, already clean and washed aluminium hydroxide is filtered and manually' transferred to drying in the dryer 39. the water phase is drained to the NaCl crystallizing ' unit 27.
• the aluminium hydroxide dryer 39 contains tub heated with service water from the hot service water reservoir 35.
• packing and distribution point 33 Al(OH) 3j water steams are exhausted to atmosphere.
• the packing and distribution point 33 consists of a hall for warehousing of dried aluminium hydroxide intended for sale in the form requested by customer.
• the zone without hydrogen contains accessory devices such as hot service water reservoir 35.
• This is the reservoir for hot water coming from cooling of the reactor L .Hot water is distributed to the operation,, excessive water may be then used for other purposes such as drying of wood etc.
• the second reservoir 36 of hydrochloric acid is the tank for 37% hydrochloric acid used for neutralization of lye in ' the first precipitator 16 Al(OH) 3j neutralizing unit 25 and the second precipitator 29 Al(OH) 3j and for refilling of the first reservoir 15 of hydrochloric acid in the hydrogen zone:
• the second reservoir 37 of sodium hydroxide is the reservoir used for storing of operation lye .(purchased) used for neutralization in the first precipitator 16 Al(OH) 3> neutralizing unit 25 and the second precipitator 29 Al(OH) 3> and for refilling of the first reservoir 20 of sodium hydroxide in the hydrogen zone.
• the method and device according to the invention can be used for the industrial production of hydrogen and other produpts from waste aluminium materials in various forms, whereas the hydrogen and other products are purified to a condition suitable for subsequent industrial use.

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