This invention describes a method for production of aluminium with near zero net CO ₂ emissions. More specific, the aluminium is to be produced by electrolysis of aluminium trichloride, AICI ₃ . Production of this AICI ₃ and recycling of the carbon used in the production of the AICI ₃ is included in the production method. The carbon recycling ensures near zero net CO ₂ emissions.

The sole commercial process for aluminium production is the so-called Hall-Heroult process, named after its inventors. In this process smelter grade alumina (AI2O3) is dissolved in a molten fluoride electrolyte and electrolyzed using carbon anodes. The anode product is CO2, where the oxygen comes from the dissolved alumina and the carbon from the carbon anode itself. The net reaction for the Hall-Heroult process is AI2O3 + 1 5C = 2AI + 1.5 CO2.

It is well known in the prior art that it is also possible to produce aluminium according to the so-called Alcoa chloride process. In this process smelter grade alumina is coked (US381 1916). The coked alumina is then undergoing chlorination according to the reaction Al ₂ 03(s) + 3Cl ₂ (g) +1.5C(s) = 2AICi ₃ (g) + 1.5C0 ₂ (g) (US4083928) followed by separation of CO2 and AICI3 by cooling and condensation of the AICI3 (US4070488). The AICI3 thus produced is fed to an electrolysis cell where the AICI3 dissolves in a molten chloride melt. Aluminium metal is formed on the cathode and chlorine gas on the anode: AICI3 = Al(l) + 1 5CI (g) The chlorine is recycled to the chlorination step and the metal extracted for further treatment and casting. The net reaction for the process is AI2O3 + 1.5C = 2AI + I .5CO2, the same as for the Hall-Heroult process. The CO2 emission for both processes is about 1.5 kg CO2 for each kg of Al produced. Although developed to industrial scale, the chloride process was never applied for commercial production of aluminium.

It is also known that it is possible to perform the chlorination of alumina using gaseous CO instead of carbon: A 03(s) + 3C (g) +3CO(g)= 2AICl ₃ (g) + 3C0 ₂ (g). It is reported that this reaction is faster than when using carbon (e.g. US4957722). If the CO used for the chlorination comes from carbon sources outside the process, e.g. by partial oxidation of carbon or natural gas, the CO based chlorination leads to two times larger CO2 emissions than the carbon-based chlorination. To achieve the goal of this invention, i.e. near zero net CO2 emissions, it is therefore important to minimize the use of fossil carbon sources for the CO gas. Direct electrochemical conversion of CO ₂ to CO and oxygen has been described in the scientific literature for over a century (see e.g. Jitaru et al, J. Appl. Electrochem., Vol 27, p. 875, 1997 and references therein). During the last decades, the technology has gained renewed scientific and commercial interest. The basic principle is that CO ₂ is reduced on a cathode to CO, e.g.: CO ₂ + 2e + H ₂ 0 = CO + 20H- in aqueous electrolytes or C0 ₂ + 2e = CO + O ² in a solid oxide electrolyte. On the anode, there is an oxidation reaction typically leading to formation of oxygen giving the net reaction CO ₂ = CO + O.5O ₂ . Electrolyzers based on modern water electrolyzers can now effectively convert CO ₂ to CO and oxygen (see e.g. US20180023198A1 ). The energy input is electricity.

According to the present invention a CO ₂ to CO reduction step is integrated with the production of AICI ₃ . The CO ₂ produced during the chlorination of alumina (Al ₂ 0 ₃ (s) + 3CI (g) +3CO(g)= 2AICl ₃ (g) + 3C0 ₂ (g)) shall be reduced to CO. The CO thus produced is fed to the chlorination together with alumina and chlorine. This integration ensures internal recycling of carbon in the process, thereby nearly eliminating CO ₂ emissions. CO ₂ can be reduced to CO in several ways. Direct electrochemical reduction, CO ₂ = CO + O.5O ₂ , where CO is produced on the cathode and oxygen is produced on the anode, is shown above. Another example is hydrogen reduction of CO ₂ : CO ₂ + H ₂ = CO + H ₂ O, the so-called reverse water gas shift reaction. To ensure close to zero CO ₂ emissions, the electricity and hydrogen used for CO ₂ reduction should come from non-C02 emitting sources. Examples are electricity produced by from renewable wind, solar or hydro power, and hydrogen produced by water electrolysis using the same sources for the electricity.

It is also possible to use hydrocarbons to reduce the CO ₂ . There will then be C0 ₂ emissions, but smaller than from the present state-of-the-art, the Hall-Heroult process.

These and further steps can be achieved by the invention according to the accompanying claims.

According to one aspect of the invention, there is described a novel process for production of aluminium (Al) by electrolysis of aluminium chloride (AICI ₃ ), wherein the aluminium chloride (AICI ₃ ) is produced from an aluminium oxide (AI ₂ O ₃ ) containing feedstock by reaction with carbon monoxide (CO) and chlorine (CI ₂ ), and where carbon dioxide (CO ₂ ) formed in this reaction is subsequently reduced to carbon monoxide (CO), wherein the said carbon monoxide (CO) is recycled to the aluminium chloride (AICI ₃ ) production and wherein the electrolysis of the aluminium chloride (AICI ₃ ) forms aluminium metal (Al) and chlorine (CI ₂ ), and where this chlorine (C ) is recycled to the aluminium chloride (AICI ₃ ) production. According to other aspects of the invention, the CO2 is reduced by electrolysis, in reaction with hydrogen, natural gas or with a hydrocarbon.

The invention will be further explained by example and Figure as follows;

Fig. 1 discloses a simplified process diagram of the process steps in one embodiment of the invention.

The various steps in the overall process is described by the following chemical reactions:

The process steps above are shown schematically in a simplified process flow diagram, Fig 1 . A description of the main steps and some alternative embodiments thereof in the process are given in the following.

Alumina chlorination:

In this step reaction 1 is taking place. Here alumina, chlorine and carbon monoxide are brought together in a suitable chlorination reactor. The alumina is preferably fed as powder or particles. A suitable reactor is a fluidized bed reactor. The operating temperature can be around 700°C. The conversion of the reactants to AICI3 and CO2 is close to 100%, but there will be traces of unreacted alumina, chlorine and CO as well as other reaction products.

Chlorination off-gas treatment:

The off-gas from the chlorination is not only AICI3 and CO2. There will also be unreacted alumina dust, CO and CI2, as well as products from impurities in the unreacted alumina dust, chlorine and CO. There may also be traces of reactor materials. To ensure high quality AICI3 feed to the electrolysis cell, the off-gas components must be separated. The alumina dust can be separated by a cyclone or filter. Some of the chlorinated impurities from the alumina, such as sodium and calcium, are much less volatile than the aluminium chloride. Due to some hydrogen content in the alumina, there will also be formation of HCI gas. By cooling the offgas to a temperature above the condensation point of the AICI3 (>180°C), several of the off- gas impurities will condensate, allowing for removal by e.g. filtration. After these initial separation steps, the off-gas is mainly AlC and gases with a lower condensation temperature, including CO2. The AICI3 can therefore be condensed to a nearly pure solid by further cooling to a temperature somewhat below the condensation point. The reactor for this condensation must be able to extract all the heat released during the AICI3 condensation and allow for removal of the condensed material without contact with ambient atmosphere. AICI3 hydrolyses immediately when contacted with moisture.

A suitable reactor can be one where the gas is led into a bed of fluidized AICI ₃ particles. The bed is internally cooled, and the fluidization gas is some of the CO ₂ that has left the fluidized bed reactor. The gaseous AICI ₃ entering the reactor condenses on the fluidized AICI ₃ particles. Particles are removed from the reactor. Undersized particles are returned to the reactor to allow for further growth. The remaining particles are handled and stored in a dry atmosphere until they are fed to the electrolysis cells.

The gaseous species remaining after AICI ₃ condensation, mainly CO2, must be treated further before the CO2 can be reduced to CO. Standard gas treatment technologies such as filters and scrubbers are sufficient. The final off-gas is C0 ₂ suitable as feed for the C0 ₂ reduction step.

CO production from CO2:

CO2 can be reduced to CO in several ways. The reduction is quite energy intensive, with a theoretical minimum requirement at 25°C of 1.8 kWh pr kg C0 reduced. In view of the purpose of the invention described here, i.e. to minimize CO2 emissions from fossil sources during aluminium production, the reduction method should preferably not involve the consumption of fossil carbon-based materials, neither as chemicals nor sources of energy. Preferred methods are the electrochemical (reaction 2a) and the hydrogen reduction routes (reaction 2b), which allow for use of electricity produced from renewable sources as the main energy input.

Direct electrochemical conversion of CO2 to CO and oxygen can be applied. The basic principle is that CO2 is reduced on a cathode to CO, e.g.: CO2 + 2e + H2O = CO + 20H-. On the anode, the hydroxide is oxidized: 20H- = 0.5O ₂ + H ₂ 0 + 2e-. The net reaction is C0 ₂ = CO + 0.5O ₂ . Electrolyzers based on modem water electrolyzers can now effectively convert CO2 to CO and oxygen where the energy input is electricity. Hydrogen reduction of CO2 may also be one alternative. The reverse water gas shift reaction, CO2 + H2 = CO + H2O, is one example. The reaction is mildly endothermic and CO2 conversion is favoured at high temperatures. The reaction is not completely shifted to the right, so the CO must be separated from the other gases, e.g by membranes, before use in the chlorination step. The hydrogen required can be produced by water electrolysis using renewable electricity.

Hydrocarbons can also be used to reduce the CO ₂ . However, not without CO ₂ emissions, but with significant reduction compared to the state-of-the-art Hall-Heroult process. An example is reduction by methane: 3CO ₂ + 0.75CH ₄ = 3CO + 0.75CO ₂ + I .5H ₂ O. The carbon from the methane is let out of the process as CO ₂ . The net reaction for the full process, starting from alumina and natural gas, will be AI2O ₃ + O.75CH ₄ = 2AI + 0.75 CO2 + I .5H ₂ O, i.e. half the CO ₂ emissions compared to the Hall-Heroult net reaction. electrolysis:

The aluminium metal is produced in an electrolysis cell. The main principle is that the aluminium chloride is added to an electrolyte consisting of a mixture of molten non-aqueous alkali and alkali earth chlorides. The operating temperature of the cell is above the melting point of aluminium, 660°C. It is possible to use graphite as anode and cathode. On the cathode, AICI3 is reduced to liquid aluminium metal: AICI3 + 3e = Al(l) + 3CI-. On the anode, the chloride in the molten electrolyte is oxidized to chlorine gas: 3CI- = 1.5 Cl2(g) + 3e-. The net reaction is AICI3 = Al(l) + 1.5 Ch(g). To minimize the energy consumption during electrolysis, a bi-polar electrode configuration can be advantageous. The liquid aluminium is extracted from the cell at regular intervals and cast to suitable products. The chlorine is treated to remove volatile electrolyte components and then transferred to the alumina chlorination step. The volatile electrolyte components are completely or partially returned to the electrolysis cell.