Patent Application
20250101606
The present disclosure relates to desulfurisation of gasses.
The majority of biogas plants use either activated carbon, iron chloride, or a biological scrubbing system for removal of H2S. Biogas desulfurization is required, no matter the downstream application, due to the harmful properties of H2S. These include corrosion, health issues, and inactivation of catalysts by H2S.
While other desulfurization technologies removes sulfide downstream of the digester once it has transformed to H2S, the iron chloride process removes the sulfide inside the digester. Iron salt, most often iron chloride, is added to the digester in a solution, which limits the H2S production through the formation of iron-sulfides. While the primary advantage of this technology is the lack of capital expenditure, as the dosing of the liquid FeCl2 can be done in a simple way compared to the construction of scrubbers, the disadvantage is the high operating expense, as FeCl2 has to be continuously added to the digester.
Activated carbon, or impregnated activated carbon, has found application within odor control and gas purification. The ability to remove impurities down to very low levels, makes the activated carbon a widely used technology for polishing or trace amount desulphurization. However, the price of activated carbon during operation makes it an expensive choice for bulk desulphurization, and when saturated, the activated carbon needs either to be regenerated or exchanged leading to substantial expenses.
The operational expenses associated with H2S removal using a biological scrubber are lower compared to the two alternatives above. The sulfur eating bacteria requires only nutrients and air to remove the H2S. Therein, however, lies one of the weaknesses of the process, as the addition of air results in an increased oxygen (O2) content in the downstream biogas. This is a serious issue for biogas plants with upgrading facilities, as the natural gas grid only allows for very low levels of O2. Another issue with the biological scrubbing systems are the lack of flexibility, as both too little and too much H2S will kill the bacteria. The lack of flexibility combined with the addition of oxygen to the cleaned biogas results in unwanted downtime.
Chlorine-based bleaches have also been used for desulfurization of gasses. However, the use of hypochlorite can introduce undesired chlorine into the gas, effectively replacing one undesired contaminant for another. The operation parameters are especially sensitive to the amount of H2S in the gas to be purified, requiring constant monitoring and adjustment in response to the H2S content in order to achieve effective desulfurization of the gas, and to avoid introduction of undesired chlorine. These plants may also suffer from high operational costs due to the need for continuous addition of bleach.
The present disclosure describes a system and a method for cleaning of gas, such as fuel gasses. Particularly, the disclosure provides a system and a method for desulfurization of gases. The disclosed invention has a low operating cost, in part because it requires relatively small volumes of liquid for its operation compared to the volume of the gas purified and/or the amount of contaminant removed from said gas. This is achieved by recycling and regeneration the scrubbing liquid electrochemically. The system is also capable of using inexpensive reagents for desulfurization, further contributing to the low operation expenses. Furthermore, because the system is capable of regenerating the desulfurization agent, it is less dependent on continuous maintenance.
One aspect of the present disclosure provides for a system for desulfurisation of gas, said system comprising:
One aspect of the present disclosure provides a system, wherein:
One aspect of the present disclosure provides for a method of desulfurising gas, said method using the system disclosed herein.
On aspect of the disclosure provides for a method for desulfurisation of gas, said method comprising the steps of
In one further aspect of the disclosure, step vii. further comprises a step of:
One aspect of the present disclosure provides for a fuel gas processing plant comprising the system as disclosed herein.
One aspect of the disclosure provides for a system configured for performing the method as disclosed herein.
By “electrolysis element” is meant an element capable of consuming electrical energy to convey a chemical change in a chemical composition. An electrolysis element includes electrochemical cells, electrolytic cells, such as electrolytic diaphragm cells.
By chlorine is meant Cl2′ unless otherwise specified.
By hypochlorite is meant the ion ClO−, which may be present in an aqueous solution together with a suitable counter ion, for example H+ or Na+.
As used herein, once a scrubbing liquid has been passed through a wet scrubbing element, it is termed a “spent scrubbing liquid”. However, such liquid may still possess capacity for performing wet scrubbing. As used herein “Scrubbing liquid” comprises “spent scrubbing liquid”, “anolyte” and “catholyte”. “Spent scrubbing liquid” may comprise components found in the anolyte and the catholyte, and may thus still have some capacity for carrying out the wet scrubbing disclosed herein.
By “desulfurisation” is meant a reduction in the content of sulfur compounds, such as a reduction of H2S content.
As used herein, “gas” comprises gases that are substantially a single type of compound and also mixtures of two or more gasses. The gasses may comprise one or more contaminants, such as one or more sulfur compounds. The gasses disclosed herein are preferably gasses in the temperature range of 0 to 100° C.
It is contemplated that whenever a sodium ion species, such as NaCl, NaOH, or NaClO, as described herein, such species may be substituted with the corresponding species of other alkali metals or earth alkali metals, such as potassium, lithium, or calcium or other cationic species such as other metal ions, other inorganic cations, and organic cations. The term “organic cation” refers to a cation comprising carbon. The cation may comprise further elements, for example, the cation may comprise hydrogen, nitrogen or oxygen. The term “inorganic cation” includes any metal cations, including the s-block metals, d-block metals, and p-block metals, and ammonium. Exemplary species suitable to carry out the disclosed invention is NaCl, NaOH, NaClO, KCl, KOH, KClO, LiCl, LiOH, LiClO, MgCl2, Mg(OH)2, Mg(OCl)2, CaCl2, Ca(OH)2, Ca(OCl)2, BaCl2, Ba(OH)2, Ba(OCl)2. That is, it is the anionic species that aids in the desulfurisation of gasses as disclosed herein. The cationic species (Na+, K+, Li+, etc.) are considered spectator ions, and can be substituted for other cationic species which do not negatively effect the desulfurisation of the gas.
As used herein, the term “electrolysis element” refers to any element capable of carrying out electrolysis of an aqueous liquid, such as an aqueous solution. Specifically, such electrolysis is the conversion of one or more chemical components of the aqueous solution to one or more other chemical components, said conversion being carried out using electrical energy. In a specific embodiment, the electrolysis element is an electrochemical cell.
The electrolysis element of the present disclosure comprises two electrodes: the anode carries out oxidation of the one or more chemical components of said aqueous solution to produce an anolyte; the cathode carries out reduction of one or more chemical components of said aqueous solution to produce a catholyte. One embodiment of the present disclosure provides for an electrolysis element comprising separate compartments for generation of anolyte and catholyte. Such construction allows for anolyte and catholyte to be separately obtained from said electrolysis element. The electrolysis element of the present disclosure alternatively provides for an electrolysis element comprising a single compartment for generation of anolyte and catholyte. Such constructions allows for obtaining the anolyte and catholyte as a mixture.
The electrolysis element of the present disclosure may comprise separate liquid inlets to the anolyte and catholyte compartments. This construction allows for introduction to the catholyte compartment of a liquid already enriched in a chemical species which is produced in the catholyte compartment. For example, as disclosed herein, the cathode may produce hydroxide ions as a chemical species. If a liquid already enriched in hydroxide ions is introduced to the catholyte compartment, said liquid may be further enriched in hydroxide ions. This construction also allows for introduction to the anolyte compartment of a liquid already enriched in a chemical species which is produced in the catholyte compartment. For example, as disclosed herein, the anode may produce chlorine as a chemical species. If a liquid already enriched in chlorine is introduced to the anolyte compartment, said liquid may be further enriched in chlorine. Thus, in one embodiment of the present disclosure, the electrolysis element comprises separate liquid inlets to the anolyte and catholyte compartments.
The electrolysis element of the present disclosure may comprise a liquid inlet supplying both the anolyte and the catholyte compartments. This construction allows for introduction to the catholyte compartment and/or the anolyte compartment of a liquid already enriched in either of a chemical species generated at the cathode and/or a chemical species generated at the anode to be further enriched in any of such chemical species. This construction also allows for introduction of liquid comprising a compound which is converted by both the anode and the cathode. By way of example, an aqueous solution of NaCl would be converted to an aqueous solution of chlorine at the anode, whereas it would be converted to an aqueous solution of sodium hydroxide at the cathode. Thus, in one embodiment of the present disclosure, the electrolysis element comprises one liquid inlet.
In one embodiment of the present disclosure, the electrolysis element is an electrolytic cell for conducting an electrochemical process wherein an electrolyte is passed through a microporous diaphragm that separates the anolyte and catholyte compartments of the cell. In response to an electrical field that is generated between an anode contained in the anolyte compartment and a cathode contained in the catholyte compartment, the electrolyte is dissociated to synthesize other chemical materials, e.g., inorganic materials. In one aspect, the electrolytic cell is a chloralkali diaphragm cell wherein, for example, aqueous sodium chloride brine undergoes electrolysis to produce sodium hydroxide in the catholyte compartment and chlorine gas in the anolyte compartment.
As used herein, Nm3/h means normal cubic meters per hour. By “normal” is meant under standard conditions, e.g. at 1 atm and 0° C. Whenever, a parameter is designated in Nm3/h, it is also intended that said parameter is given in m3/h.
In one embodiment, the electrolysis element comprises one liquid inlet configured to supply the anolyte compartment and another liquid inlet supplying the catholyte compartment.
The anolyte as disclosed herein comprises an oxidising agent. In one embodiment, the oxidising agent is produced in the anolyte compartment of the electrolysis element. In one embodiment of the present disclosure, the oxidising agent is a chlorine-based bleaching agent. In a specific embodiment, the oxidising agent is capable of oxidising H2S to sulfur of at least oxidation number 0, such as elemental sulfur. In another embodiment, the oxidising agent is capable of oxidising H2S to sulfur having an oxidation number higher than 0, such as +2, +4, or +6. In one embodiment, the oxidising agent is capable of oxidising H2S to sulfate, such as sulfate ions. In one embodiment of the present disclosure, the oxidising agent is chlorine. In aqueous solution, chlorine undergoes conversion to other species by reaction with water. Such species are for example hypochlorite. In one embodiment, the oxidising agent is hypochlorite ions. In a particular embodiment of the present disclosure, the oxidising agent is a mixture of chlorine and hypochlorite ions. In one embodiment of the present disclosure, the anolyte is generated from aqueous sodium chloride.
The catholyte as disclosed herein comprises a compound capable of removing chlorine a gas, for example by scrubbing the gas and/or converting the chlorine to another chemical species. The catholyte is generated in the catholyte compartment of the electrolysis element. Suitable catholyte components include hydroxide ions. In one embodiment, the catholyte comprises hydroxide ions, for example as sodium hydroxide, potassium hydroxide, lithium hydroxide or other alkali hydroxides, magnesium hydroxide, calcium hydroxide, barium hydroxide, or other earth alkali hydroxides, or hydroxides of d-block elements or hydroxides of p-block elements. Hydroxide ions react with chlorine to produce hypochlorite ions. In one embodiment of the present disclosure, the catholyte is generated from aqueous sodium chloride.
As disclosed in the examples herein, the presence of hydroxide ions in the catholyte effects efficient removal of chlorine from the gas. The reaction is stoichiometric with respect to hydroxide ions and chlorine. The reaction proceeds even at low concentration of hydroxide ions.
The wet scrubbing element as disclosed herein is capable of facilitating a high surface area contact between a liquid and a gas, thereby facilitating transfer of certain chemical components from said gas to said liquid (scrubbing liquid). Such chemical components may be sulfur compounds (e.g. H2S). Furthermore, reactive species in the scrubbing liquid may react with chemical components of the gas, thereby further facilitating transfer to the scrubbing liquid. This is for example achieved by conversion from chemical species that are gaseous to chemical species that are not, such as solid, liquid, or ionic species.
In one embodiment of the present disclosure, the wet scrubbing element is a wet scrubbing tower. The wet scrubbing tower may have any suitable configuration that allows for contact between the gas and the scrubbing liquid. Wet scrubbing towers will typically be packed with a packing material or comprise an internal structure, both of which can facilitate dispersion of the scrubbing liquid to provide a high surface contact between said liquid and the gas. The present inventors contemplate that other means facilitating the contact of the liquid and the gas may also be used in the system of the present disclosure.
In one embodiment of the present disclosure, the gas is supplied essentially at the bottom of the wet scrubbing tower at a gas inlet and let out essentially at the top of the wet scrubbing tower at a gas outline. This creates a counter flow between the ascending gas the descending scrubbing liquid, which can improve the scrubbing efficiency.
In one embodiment of the present disclosure, the anolyte is supplied to the scrubbing tower via an anolyte inlet. In one embodiment, the catholyte is supplied to the scrubbing tower via a catholyte inlet. In one embodiment, the scrubbing tower comprises one or more scrubbing liquid outlets. One embodiment provides for a configuration of anolyte and catholyte inlets and scrubbing liquid outlets as shown in
In one embodiment of the present disclosure, the catholyte inlet is positioned downstream of the anolyte inlet relative to the direction of the gas flow.
In one embodiment, the system of the present disclosure comprises two wet scrubbing towers, wherein the anolyte inlet and catholyte inlets are position on separate wet scrubbing towers, and wherein the catholyte inlet is position on the tower downstream of the tower on which the anolyte inlet is positioned, relative to the direction of the flow of the gas through the two wet scrubbing towers.
A part of the catholyte may be introduced together with the anolyte liquid. Specifically, in one embodiment of the present disclosure, 1 to 10%, 10 to 20%, 20 to 30%, 30 to 40%, 40 to 50%, 50 to 60%, 60 to 70%, 70 to 80%, 80 to 90%, or 90 to 100% of the catholyte liquid may be introduced at the anolyte inlet.
The wet scrubbing elements, e.g. the wet scrubbing towers, of the present disclosure comprises one or more scrubbing liquid outlets. In one embodiment of the present disclosure, the scrubbing liquid outlet is positioned essentially at the bottom of the wet scrubbing element. In one embodiment of the present disclosure, the wet scrubbing element comprises a scrubbing liquid outlet between the catholyte inlet and the anolyte inlet. In one embodiment, the wet scrubbing element comprises a scrubbing liquid outlet between the catholyte inlet and the anolyte inlet and a scrubbing liquid outlet below the anolyte inlet.
In one embodiment, the system of the present disclosure comprises two wet scrubbing elements, wherein the first wet scrubbing element comprises an anolyte inlet and a scrubbing liquid outlet, and the second wet scrubbing element comprises a catholyte inlet and a scrubbing liquid outlet.
The scrubbing liquid of the present disclosure is generated from a suitable aqueous composition. In one embodiment, the scrubbing liquid comprises or is generated from a liquid comprising chloride ions. In one embodiment, the source of the chloride ions is a chloride salt. The chloride salt may be any suitable chloride salt. In one embodiment, the cation in the chloride salt is an inorganic cation. In one embodiment, the cation is a metal cation. In one embodiment, the metal of the metal cation is an s-block metal, a d-block metal, or a p-block metal. In one embodiment, the cation is an ammonium cation. In one embodiment the cation is an organic cation, such as a monoalkyl, dialkyl, trialkyl, or tetraalkyl ammonium ion. In one embodiment, the cation comprises carbon. In a further embodiment, the cation further comprises other elements than carbon, for example, the cation may comprise hydrogen, nitrogen or oxygen. In on embodiment, the cation is chosen so that it does not interfere with the electrochemical reactions and/or redox reactions occurring in the system of the disclosure, e.g. the cation is a spectator ion. In one embodiment, the chloride salt is soluble in aqueous solution. In one embodiment of the present disclosure, the cation is selected from Li+, Na+, K+, Mg2+, Ca2+, Sr2+, Ba2+ and metal ions of the d-block and metal ions of the p-block.
In one embodiment of the disclosure, the scrubbing liquid is generated from a mixture of cation hydroxide, wherein the cation is as disclosed herein, and hydrochloric acid. In one embodiment of the disclosure, the cation hydroxide and the hydrochloric acid is mixed in substantially equimolar ratio.
In one embodiment of the present disclosure, such composition is an aqueous solution of a chloride salt. In one embodiment, such composition comprises from 1 g/L chloride ions to saturation in chloride.
In on embodiment of the present disclosure, such composition is an aqueous solution of a chloride salt, such as an alkali chloride salt. In one embodiment, such composition is an aqueous sodium brine (NaCl) composition. In one embodiment, the scrubbing liquid comprises between 1 and 300 g/L NaCl, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L NaCl. In one embodiment, such composition has a NaCl concentration between 0.1 g/L and saturation. In one embodiment, such composition is an aqueous potassium chloride composition. In one embodiment, the scrubbing liquid comprises between 1 and 300 g/L KCl, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L KCl. In one embodiment, such composition has a KCl concentration between 0.1 g/L and saturation. In one embodiment, such composition is an aqueous lithium chloride composition. In one embodiment, the scrubbing liquid comprises between 1 and 300 g/L LiCl, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L LiCl. In one embodiment, such composition has a LiCl concentration between 0.1 g/L and saturation. In one embodiment, such composition is an aqueous earth alkali chloride composition. In one embodiment, the scrubbing liquid comprises between 1 and 300 g/L earth alkali chloride, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L earth alkali chloride. In one embodiment, such composition has an earth alkali chloride concentration between 0.1 g/L and saturation. In one embodiment, the scrubbing liquid comprises between 1 and 300 g/L chloride salt, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L chloride salt. In one embodiment, such composition has a chloride salt concentration between 0.1 g/L and saturation.
One embodiment of the present disclosure provides for a scrubbing liquid generated in the anolyte compartment of the electrolysis element. Such scrubbing liquid is also termed “anolyte” herein. In one embodiment, the anolyte comprises one or more of the species selected from the group consisting of: chlorine, hypochlorite ions, chloride ions, and sodium ions. In one embodiment of the disclosure, the anolyte comprises chlorine, hypochlorite ions, chloride ions, and sodium ions.
One embodiment of the present disclosure provides for a scrubbing liquid generated in the catholyte compartment of the electrolysis element. Such scrubbing liquid is also termed “catholyte” here. In one embodiment, the catholyte comprises one or more of the species elected from the group consisting of: hydroxide ions, chloride ions, and sodium ions. In one embodiment, the catholyte comprises hydroxide ions, chloride ions, and sodium ions.
One embodiment provides for a scrubbing liquid generate in both the anolyte compartment and the catholyte compartment of the electrolysis element. Such scrubbing liquid comprises both anolyte and catholyte.
In one embodiment of the present disclosure, the anolyte and catholyte are mixed within the wet scrubbing element. In one embodiment of the present disclosure, the anolyte and catholyte are not mixed within the one or more wet scrubbing elements. In one embodiment, the spent anolyte and spent catholyte are drained separately from the one or more wet scrubbing and subsequently kept separate.
The present disclosure provides a system for desulfurisation of gases. The system of the disclosure uses a relatively low amount of solvent, such as water, because the scrubbing liquid is continuously recycled. Specifically, after being drained from the wet scrubbing element(s), the scrubbing liquid is electrochemically regenerated in the electrolysis element, after which is may be reapplied to the wet scrubbing elements.
The recycling of the wet scrubbing liquid is also facilitated by the choice of scrubbing liquid. Specifically, if the anolyte and catholyte are generated from an aqueous solution of chloride ions, the scrubbing of H2S by generated chlorine/hypochlorite will produce chloride ions, which can be converted to chlorine/hypochlorite. Regarding the catholyte, hydroxide ions react with chlorine in the gas to generate hypochlorite, which in turn are converted to chloride ions upon reaction with H2S. This allows for only an initial amount of aqueous solution of chloride ions (e.g. NaCl) in a finite volume to be supplied to the system, after which the system can carry out desulfurisation for extended periods of time. This effects that a large volume of gas can be desulfurised with a relatively small liquid and chemical volume. This provides a clear advantage over other desulfurisation plants, which may not recycle the scrubbing liquids, and/or which may be dependent on refilling with desulfurisation and/or dechlorination agents.
The system of the present disclosure may comprise one or more bypasses of the electrolysis element. By “bypass” is meant that at least part of the spent scrubbing liquid is fed directly back to the wet scrubbing element without passing through the electrolysis element. However, this is not to be construed that the spent scrubbing liquid does not pass through other elements of the system, such as a filter or a pump, before being fed back to the wet scrubbing element. In one embodiment of the disclosure, the bypass comprises or consists of a liquid transferring element, such as a tube, a pipe, or a channel. In one embodiment electrolysis element bypass is configured to transfer liquid from the scrubbing liquid outlets to the anolyte inlet and/or the catholyte inlet by bypassing the electrolysis element.
As shown in the examples herein, the present inventors found that the efficiency of the generation of oxidising agent improves when part of the spent scrubbing liquid bypasses the electrolysis element. Thus, a bypass of the electrolysis element effects that a relatively small electrolysis element can be employed to regenerate the scrubbing liquid for even high-capacity gas scrubbing systems. Therefore, smaller electrolysis elements can be employed for even large-scale systems to desulfurize gas, saving on both the manufacture costs and the running costs of the system. Regeneration of the scrubbing liquid generally requires more energy, the higher flow is through the electrolysis element. Accordingly, the presence of the bypass allows for a lower flow rate of scrubbing liquid through the electrolysis element, while allowing for a high flow rate of scrubbing liquid through the wet scrubbing element. In conventional systems lacking a bypass of the electrolysis element, the flow rate of the gas to be sulfurised is limited by the flow rate of the scrubbing liquid, which in turn is limited by the capacity of the electrolysis device.
Even if a lower efficiency for the generation of oxidising agent is accepted, having a high scrubbing liquid flow through the electrolysis element can unnecessarily stress and deteriorate the electrolysis element. Thus, it is contemplated that the presence of the bypass increases the lifetime and reduces the need for maintenance of the electrolysis element.
In one embodiment of the present disclosure, 0.1 to 99.9% of the spent scrubbing liquid is fed to the electrolysis element, whereas the remaining spent scrubbing liquid bypasses the electrolysis element. In a further embodiment, 0.1 to 75.0%, such as 0.1 to 50.0%, such as 0.1 to 25.0%, such as 0.1 to 10.0% of the spent scrubbing liquid is fed to the electrolysis element, whereas the remaining scrubbing liquid bypasses the electrolysis element. In one embodiment, 0.1 to 0.3%, such as 0.3 to 0.5%, such as 0.5 to 0.7%, such as 0.7 to 0.9%, such as 0.9 to 1.1%, such as 1.1 to 1.3%, such as 1.3 to 1.5%, such as 1.5 to 2.0%, such as 2.0 to 2.5%, such as 2.5 to 3.0%, such as 3.0 to 4.0%, such as 4.0 to 5.0%, such as 5.0 to 7.0%, such as 7.0 to 10.0% of the spent scrubbing liquid is fed to the electrolysis element, whereas the remaining scrubbing liquid bypasses the electrolysis element. In one embodiment of the present disclosure, about 1% of the spent scrubbing liquid is fed to the electrolysis element, whereas the remaining scrubbing liquid bypasses the electrolysis element. Bypassing the electrolysis element as described above allows for the use of a relatively small electrolysis element to produce and/or regenerate the oxidising agent for even large-scale desulfurisation of gas.
The bypass of the electrolysis element can be achieved in a number of ways. In one embodiment, the system of the disclosure comprises a bypass from the scrubbing liquid outlet of a wet scrubbing element to the anolyte inlet of the same or a different wet scrubbing element. In one embodiment, the system of the disclosure comprises a bypass from the scrubbing liquid outlet of a wet scrubbing element to the catholyte inlet of the same or a different wet scrubbing element. In one embodiment, the system comprises a bypass from the scrubbing liquid outlet of a first wet scrubbing element to the anolyte inlet of said first wet scrubbing element. In one embodiment, the system comprises a bypass from the scrubbing liquid outlet of a second wet scrubbing element to the catholyte inlet of said second wet scrubbing element. In one embodiment, the system comprises a bypass from the scrubbing liquid outlet of a first wet scrubbing element to the catholyte inlet of a second wet scrubbing element. In one embodiment, the system comprises a bypass from the scrubbing liquid outlet of a second wet scrubbing element to the anolyte inlet of a first wet scrubbing element. In one embodiment, the system comprises at least one bypass per scrubber. In one embodiment, the system comprises a bypass from the scrubbing liquid outlet of a first wet scrubbing element to the anolyte inlet of said first wet scrubbing element, and another bypass from the scrubbing liquid outlet of a second wet scrubbing element to the catholyte inlet of said second wet scrubbing element.
In one embodiment of the present disclosure, at least one other element is present between the scrubbing liquid outlet of the wet scrubbing element and the bypass such as one or more elements for splitting the liquid flow, one or more flow control valves, one or more pumps, and/or one or more filters.
In one embodiment of the present disclosure, the bypass is a tube or a hose. In one embodiment, the bypass may comprise one or more flow control valves, one or more pumps, and/or one or more filters.
In one embodiment of the present disclosure, the system further comprises a mixing element. The role of the mixing element is the combine and/or mix two different liquid flows. The two different liquid flows may for example be a liquid flow from the electrolysis element comprising regenerated oxidising agent and a liquid flow from the bypass comprising spent scrubbing liquid. In one embodiment, the mixing element is positioned prior to the anolyte inlet or the catholyte inlet on a wet scrubbing element
The present disclosure provides for a system for cleaning of gas. In one embodiment, said cleaning is desulfurisation. As used herein “cleaning of gas” is the reduction in content of a contaminant such as a sulfur compound.
The system of the present disclosure achieves desulfurisation of gas by wet scrubbing with an oxidising agent. As disclosed herein, the oxidising agent may be chlorine-based, such as chlorine (Cl2) and/or hypochlorite. It is an issue that desulfurisation using chlorine-based oxidants can introduce chlorine to the gas. It is detrimental having gasses such as fuel gasses contaminated with chlorine, as said chlorine can be incorporated in combustion products. Introduction of chlorine may for example occur when the content of H2S in the inlet gas decreases, whereby the excess desulfurisation agent (Cl2) will enter the gas from the scrubbing liquid. On the other hand, should the content of H2S in the gas suddenly increase, the capacity of the desulfurisation plant may not be sufficient to effective desulfurise said gas. These aspects typically provides desulfurisation plants which are very sensitive to the amount of H2S in the inlet gas, and as a result, parameters such as H2S concentration and pH must continuously be monitored and operation parameters adjusted in response to obtain sufficiently desulfurised gas and to avoid introduction of chlorine. Furthermore, chlorine that has been introduced to the gas must be removed, which may require large volumes of additional scrubbing liquid. These aspects can dissuade the industry from using chlorine-based oxidants.
In one embodiment, the disclosed system is configured to desulfurise gas. In one embodiment, the system of the disclosure is configured to full or partial removal of one or more sulfur compounds from the gas.
As outlined herein, the system of the disclosure carries out desulfurisation by a first wet scrubbing of the gas to remove sulfur compounds (upstream in gas flow), and a second wet scrubbing to remove chlorine (downstream in gas flow).
The system of the present disclosure is especially efficient for obtaining effective desulfurisation of gas while ensuring little to no chlorine content to the desulfurised gas. As outlined herein, the system of the disclosure is also robust, requiring little to no adjustment of operating parameters in response to varying H2S content in the inlet gas. This robustness is achieved by using a first and a second scrubbing liquid, both of which are recycled, and regenerated electrochemically in the system of the disclosure.
Specifically, it is an advantage that the system of the disclosure can be run with a constant current applied to the electrolysis element. This current can be estimated based on an approximation of the H2S content of the gas in combination with the gas flow. In one embodiment of the present disclosure, the system carries out a first scrubbing of the gas to remove substantially all H2S. This is achieved by wet scrubbing with a scrubbing liquid comprising a chlorine-based oxidising agent. In one embodiment, this scrubbing liquid is the anolyte as disclosed herein. In a further embodiment, the gas undergoes a second scrubbing (which may occur downstream in the same wet scrubbing element or may occur downstream in a second wet scrubbing element) with a scrubbing liquid capable of removing any chlorine that may have been introduced to the gas during the first scrubbing. In one embodiment, said scrubbing liquid is the catholyte as disclosed herein. As disclosed in the examples below, hydroxide ions are particularly efficient in facilitating removal of chlorine from gasses. As disclosed herein, the anolyte and the catholyte may be produced in parallel by the same electrolysis element, thus supplying both the first scrubbing liquid and the second scrubbing liquid by regenerating spent scrubbing liquid. This eliminates the need for supplying any other agents or reagents to the system during its operation.
The system of the present disclosure is robust to both an increase or a decrease in H2S content of the inlet gas for the following reasons: i) Assuming the content of H2S in the inlet gas suddenly decreases and/or that the content of H2S in the inlet gas is below what was initially estimated, the electrolysis element of the system of the disclosure produces and excess oxidising agent, which may be introduced to the gas during desulfurisation. However, the downstream introduction of the second scrubbing liquid (i.e. catholyte) effectively removes any chlorine that was introduced, as evidenced by the examples herein below. ii) Assuming the content of H2S in the inlet gas suddenly increases and/or that the content of H2S in the inlet gas is above what was initially estimated, the electrolysis element may not produce enough oxidising agent (chlorine/hypochlorite) to completely desulfurise the inlet gas during the first scrubbing. However, as the gas passes through the second scrubbing, chlorine previously extracted in the secondary scrubber (and which may be continuously recycled through the second scrubber due to the bypass disclosed herein) acts to remove any H2S not removed during the first scrubber. In essence, the second scrubber acts as a buffer, extracting chlorine during periods where the electrolysis device produces and excess of oxidising agent, and removing H2S during periods where the electrolysis device produces a deficit of oxidising agent.
In one embodiment of the disclosure, the gas comprises between 1 and 100000 ppm H2S prior to being desulfurised. In one embodiment of the disclosure, the gas comprises between 1 and 10000 ppm H2S prior to being desulfurised. In one embodiment, the gas comprises between 1 and 1000 ppm H2S prior to being desulfurised. In one embodiment, the gas comprises 1 to 2 ppm H2S, 2 to 3 ppm H2S, 3 to 5 ppm H2S, 5 to 10 ppm H2S, 10 to 20 ppm H2S, 20 to 50 ppm H2S, 50 to 100 ppm H2S, 100 to 200 ppm H2S, 200 to 500 ppm H2S, 500 to 1000 ppm H2S, 1000 to 2000 ppm H2S, 2000 to 5000 ppm H2S, or 5000 to 10000 ppm H2S prior to being desulfurised.
In one embodiment of the disclosure, desulfurisation comprises removing at least 10%, such as at least 20%, such as at least 30%, such as at least 40%, such as at least 50%, such as at least 60%, such as at least 70%, such as at least 80%, such as at least 90%, such as at least 95%, such as at least 96%, such as at least 97%, such as at least 98%, such as at least 99% of the initial sulfur content of the gas. In one embodiment of the disclosure, desulfurisation comprises removing at least 10%, such as at least 20%, such as at least 30%, such as at least 40%, such as at least 50%, such as at least 60%, such as at least 70%, such as at least 80%, such as at least 90%, such as at least 95%, such as at least 96%, such as at least 97%, such as at least 98%, such as at least 99% of the initial H2S content of the gas. In one embodiment of the disclosure, desulfurisation comprises removing H2S from the gas such that the gas comprises at most 100 ppm H2S, such as at most 90 ppm H2S, such as at most 80 ppm H2S, such as at most 70 ppm H2S, such as at most 60 ppm H2S, such as at most 50 ppm H2S, such as at most 40 ppm H2S, such as at most 30 ppm H2S, such as at most 20 ppm H2S, such as at most 15 ppm H2S, such as at most 10 ppm H2S, such as at most 5 ppm H2S, such as at most 4 ppm H2S, such as at most 3 ppm H2S, such as at most 2 ppm H2S, such as at most 1 ppm H2S.
In one embodiment of the disclosure, the desulfurisation as disclosed herein is achieved while introducing to said gas at most 100 ppm Cl2, such as at most 90 ppm Cl2, such as at most 80 ppm Cl2, such as at most 70 ppm Cl2, such as at most 60 ppm Cl2, such as at most 50 ppm Cl2, such as at most 40 ppm Cl2, such as at most 30 ppm Cl2, such as at most 20 ppm Cl2, such as at most 10 ppm Cl2, such as at most 5 ppm Cl2, such as at most 4 ppm Cl2, such as at most 3 ppm Cl2, such as at most 2 ppm Cl2, such as at most 1 ppm Cl2, such as essentially no Cl2.
On embodiment of the disclosure provides for a gas desulfurised using the method disclosed herein.
One embodiment of the present disclosure provides for a desulfurised gas as disclosed here comprising:
It is contemplated that the system disclosed herein is capable of being scaled to accept a wide range of gas flows and/or gas flows having a wide range of H2S of content.
The presently disclosed system is capable of accepting a wide range of gas flows while efficiently desulfurising said gas. In one embodiment, the gas flow rate is between 150 and 400000 Nm3/h. In one embodiment, the gas flow rate is up to 150 Nm3/h. In one embodiment, the gas flow rate is 1 to 2 Nm3/h, 2 to 3 Nm3/h, 3 to 5 Nm3/h, 5 to 7 Nm3/h, 7 to 10 Nm3/h, 10 to 15 Nm3/h, 15 to 20 Nm3/h, 20 to 30 Nm3/h, 30 to 40 Nm3/h, 40 to 50 Nm3/h, 50 to 70 Nm3/h, 70 to 100 Nm3/h, 100 to 150 Nm3/h, 150 to 250 Nm3/h, 250 to 500 Nm3/h, 500 to 1000 Nm3/h, 1000 to 2000 Nm3/h, 2000 to 5000 Nm3/h, 5000 to 10000 Nm3/h, 10000 to 20000 Nm3/h, 20000 to 50000 Nm3/h, 50000 to 100000 Nm3/h, 100000 to 200000 Nm3/h, 200000 to 500000 Nm3/h, 500000 to 1000000 Nm3/h, 1000000 to 2000000 Nm3/h, 2000000 to 3000000 Nm3/h, 3000000 to 4000000 Nm3/h, and/or 4000000 to 5000000 Nm3/h. In one embodiment the gas flow rate is 50 to 500 Nm3/h, such as 80 to 400 Nm3/h, such as 100 to 300 Nm3/h, such as about 150 Nm3/h. Plants such as biogas plants may requirement desulfurisation of a gas flow of about 150 Nm3/h. In one embodiment, the gas flow rate is 50000 to 1000000 Nm3/h, such a 100000 to 800000 Nm3/h, such as 200000 to 600000 Nm3/h, such as about 400000 Nm3/h. Plants such as steel plants may requirement desulfurisation of a gas flow of about 400000 Nm3/h.
The operation parameters of the presently disclosed system can be configured based on knowledge of the approximate pollutant (e.g. H2S) content of the gas and the flow rate of the gas to be desulfurised. Table 1 outlines the approximate current to apply to the electrolysis element in order to desulfurise gas having the specific content of pollutant and/or H2S concentration. The information is based on an efficiency of the electrolysis element of 25%. The current can be further modified if the electrolysis element performs with an efficiency different from 25%, i.e. to adjust the current upwards if the electrolysis element performs with an efficiency lower than 25%, or to adjust the current downwards if the electrolysis element performs with an efficiency higher than 25%.
In on embodiment, current applied to the system is 0.0040 to 0.0200 A per ppm H2S per Nm3/h gas. In one embodiment, the current applied to the system is 0.0040 to 0.0045 A per ppm H2S per Nm3/h gas, such as 0.0045 to 0.0050 A per ppm H2S per Nm3/h gas, such as 0.0050 to 0.0055 A per ppm H2S per Nm3/h gas, such as 0.0055 to 0.0060 A per ppm H2S per Nm3/h gas, such as 0.0060 to 0.0065 A per ppm H2S per Nm3/h gas, such as 0.0065 to 0.0070 A per ppm H2S per Nm3/h gas, such as 0.0070 to 0.0075 A per ppm H2S per Nm3/h gas, such as 0.0075 to 0.0080 A per ppm H2S per Nm3/h gas, such as 0.0080 to 0.0085 A per ppm H2S per Nm3/h gas, such as 0.0085 to 0.0090 A per ppm H2S per Nm3/h gas, such as 0.0090 to 0.0095 A per ppm H2S per Nm3/h gas, such as 0.0095 to 0.0100 A per ppm H2S per Nm3/h gas, such as 0.0100 to 0.0110 A per ppm H2S per Nm3/h gas, such as 0.0110 to 0.0120 A per ppm H2S per Nm3/h gas, such as 0.0120 to 0.0130 A per ppm H2S per Nm3/h gas, such as 0.0130 to 0.0140 A per ppm H2S per Nm3/h gas, such as 0.0140 to 0.0150 A per ppm H2S per Nm3/h gas, such as 0.0150 to 0.0160 A per ppm H2S per Nm3/h gas, such as 0.0160 to 0.0170 A per ppm H2S per Nm3/h gas, such as 0.0170 to 0.0180 A per ppm H2S per Nm3/h gas, such as 0.0180 to 0.0190 A per ppm H2S per Nm3/h gas, such as 0.0190 to 0.0200 A per ppm H2S per Nm3/h gas.
The amount of current required to desulfurise the gas can alternatively be expressed in amperes per g sulfur to desulfurise per hour. By “g sulfur per hour” is meant the amount of sulfur expressed g that is fed via the gas to the system per hour. Such sulfur may exist as H2S in the gas. In one embodiment, the current is 4.0 to 9.0 A per g sulfur per hour. In one embodiment, the current is 4.0 to 4.2 A per g sulfur per hour, 4.2 to 4.4 A per g sulfur per hour, 4.4 to 4.6 A per g sulfur per hour, 4.6 to 4.8 A per g sulfur per hour, 4.8. to 5.0 A per g sulfur per hour, 5.0 to 5.2 A per g sulfur per hour, 5.2 to 5.4 A per g sulfur per hour, 5.4 to 5.6 A per g sulfur per hour, 5.6 to 5.8 A per g sulfur per hour, 5.8 to 6.0 A per g sulfur per hour, 6.0 to 6.2 A per g sulfur per hour, 6.2 to 6.4 A per g sulfur per hour, 6.4 to 6.6 A per g sulfur per hour, 6.6 to 6.8 A per g sulfur per hour, 6.8 to 7.0 A per g sulfur per hour, 7.0 to 7.2 A per g sulfur per hour, 7.2 to 7.4 A per g sulfur per hour, 7.4 to 7.6 A per g sulfur per hour, 7.6 to 7.8 A per g sulfur per hour, 7.8 to 8.0 A per g sulfur per hour, 8.0 to 8.2 A per g sulfur per hour, 8.2 to 8.4 A per g sulfur per hour, 8.4 to 8.6 A per g sulfur per hour, 8.6 to 8.8 A per g sulfur per hour, and/or 8.8 to 9.0 A per g sulfur per hour. In one embodiment, the current is 5.0 to 7.4 A per g sulfur per hour, such as 5.2 to 7.2 A per g sulfur per hour, such as 5.4 to 7.0 A per g sulfur per hour, such as 5.6 to 6.8 A per g sulfur per hour, such as 5.8 to 6.6 A per g sulfur per hour, such as 6.0 to 6.4 A per g sulfur per hour, such as about 6.2 A per g sulfur per hour. The current can be further modified if the electrolysis element performs with an efficiency different from 25%, i.e. to adjust the current upwards if the electrolysis element performs with an efficiency lower than 25%, or to adjust the current downwards if the electrolysis element performs with an efficiency higher than 25%. In one embodiment, such modification is inversely proportional to the performance of the electrolysis element.
The system of the present disclosure can be configured to run at different liquid flow rates, i.e. the liquid flow rates through the one or more scrubber elements. In one embodiment, the liquid flow rate is 10 kg/h to 3000000 ton/h. In one embodiment the liquid flow rate is up to 10 kg/h, 10 to 15 kg/h, 15 to 20 kg/h, 20 to 30 kg/h, 30 to 40 kg/h, 40 to 50 kg/h, 50 to 70 kg/h, 70 to 100 kg/h, 100 to 150 kg/h, 150 to 250 kg/h, 250 to 500 kg/h, 500 to 1000 kg/h, 1000 to 2000 kg/h, 2000 to 3000 kg/h, 3000 to 5000 kg/h, 5000 kg/h to 10 ton/h, 10 to 15 ton/h, 15 to 20 ton/h, 20 to 30 ton/h, 30 to 40 ton/h, 40 to 50 ton/h, 50 to 70 ton/h, 70 to 100 ton/h, 100 to 150 ton/h, 150 to 250 ton/h, 250 to 500 ton/h, 500 to 1000 ton/h, 1000 to 1500 ton/h, 1500 to 2000 ton/h, 2000 to 3000 ton/h, 3000 to 5000 ton/h, 5000 to 70000 ton/h, 70000 to 100000 ton/h, 100000 to 150000 ton/h, 150000 to 250000 ton/h, 250000 to 500000 ton/h, 500000 to 1000000 ton/h, 1000000 to 2000000 ton/h, and/or 2000000 to 3000000 ton/h. In one embodiment, the liquid flow rate is 15 to 50 ton/h. Plants such as biofuel plants may use a liquid flow rate of 15 to 50 ton/h. In one embodiment, the liquid flow rate is 40000 to 100000 ton/h. Plants such as steel plants may use a liquid flow rate of 40000 to 100000 ton/h. As used herein, for a liquid having a density of about 1 kg/L, a flow rate given in ton/h corresponds approximately to a flow rate given in Nm3/h. For liquids having densities significantly different from 1 kg/L, it is necessarily to account for the density when converting between ton/g and Nm3/h. In one embodiment, the liquid flow rate (in Nm3/h) corresponds to between 5% and 50% of the gas flow rate (in Nm3/h). In one embodiment, the liquid flow rate (in Nm3/h) corresponds to 5 to 10%, 10 to 15%, 15 to 20%, 20% to 25%, 25 to 30%, 30 to 35%, 35 to 40%, 40 to 45%, and/or 45 to 50% of the gas flow rate (in Nm3/h). By way of example, for an embodiment of the system using a 100 Nm3/h gas flow and a 10 Nm3/h liquid flow, the liquid flow corresponds to 10% of the gas flow.
One embodiment of the present disclosure provides for a system for cleaning of gas, said system comprising:
In one embodiment of the disclosure, the anolyte compartment and the catholyte compartment supply the wet scrubbing element, said catholyte being introduced to the wet scrubbing element at a catholyte inlet which is separate and downstream from an anolyte inlet, relative to the direction of the gas flow through the one or more wet scrubbing elements, and wherein the one or more wet scrubbing elements comprise one or more scrubbing liquid outlets, said one or more scrubbing liquid outlets at least in part supplying the electrolysis element.
In one embodiment of the disclosure, the system comprises:
In one embodiment, the system comprises:
Such liquid transferring elements function to transfer liquid between the specified parts of the system. The liquid transferring elements may for example be pipes, tubes, and/or channels. The liquid transferring elements can be of any length sufficient for connecting the specified parts.
In one embodiment, the system of the disclosure comprises an electrolysis element bypass between the one or more scrubbing liquid outlets and the anolyte inlet and/or catholyte inlet. In one embodiment one or more scrubbing liquid outlets at least in part bypasses the electrolysis element to supply the wet scrubbing elements. In one embodiment, the bypass is a liquid transferring element.
In one embodiment, the system of the disclosure comprises two wet scrubbing elements connected in series with respect to the gas flow.
If the system of the disclosure comprises two or more wet scrubbing elements, the wet scrubbing element that the gas passes through first is designated the first wet scrubbing element, the element that the gas passes through second is designated the second wet scrubbing element (etc.).
In one embodiment, the gas is a fuel gas. In a further embodiment, the fuel gas is selected from the group consisting of coke-oven gas, natural gas, gas from geothermal plants, shale gas, and landfill gas.
In one embodiment, the gas is selected from the group consisting of process gas from the production of bio-technical products, e.g. pharma products, and exhaust gas from chemical factories, e.g. paint factories.
In one embodiment of the present disclosure, the electrolysis element comprises a single liquid inlet supplying both the anolyte compartment and the catholyte compartment. In one embodiment, the electrolysis element comprises a single liquid inlet configured to supply both the anolyte compartment and the catholyte compartment.
In one embodiment, the electrolysis element comprises one liquid inlet supplying the anolyte compartment and another liquid inlet supplying the catholyte compartment.
In one embodiment of the present disclosure, the one or more wet scrubbing elements are one or more wet scrubbing towers.
In one embodiment of the present disclosure, the system comprises a wet scrubbing element having a scrubbing liquid outlet, wherein said scrubbing liquid outlet is positioned between the anolyte inlet and the catholyte inlet.
In one embodiment, the scrubbing liquid outlet supply the wet scrubbing element at the anolyte inlet. In one embodiment, the scrubbing liquid outlet is configured to supply the wet scrubbing element at the anolyte inlet.
In one embodiment of the present disclosure, the scrubbing liquid outlet supply the wet scrubbing element at the catholyte inlet. In one embodiment, the scrubbing liquid outlet is configured to supply the wet scrubbing element at the catholyte inlet.
In one embodiment of the present disclosure, the scrubbing liquid outlet supply both the electrolysis element and the wet scrubbing element at the anolyte inlet. In one embodiment, the scrubbing liquid outlet is configured to supply both the electrolysis element and the wet scrubbing element at the anolyte inlet.
In one embodiment of the present disclosure, the scrubbing liquid outlet supply both the electrolysis element and the wet scrubbing element at the catholyte inlet. In one embodiment, the scrubbing liquid outlet is configured to supply both the electrolysis element and the wet scrubbing element at the catholyte inlet.
In one embodiment, part of the catholyte, but not all of the catholyte, is being introduced to the wet scrubbing element at the anolyte inlet. In one embodiment, the system is configured to introduce part, but not all of the catholyte, to the wet scrubbing element at the anolyte inlet.
One embodiment of the present disclosure provides a system, wherein:
One embodiment of the present disclosure provides a system wherein:
In one embodiment of the disclosure, the one or more wet scrubbing elements are two wet scrubbing towers.
In one embodiment of the disclosure, the one or more wet scrubbing elements is a single wet scrubbing tower.
In one embodiment, the system comprises a single wet scrubbing tower, wherein the catholyte inlet is positioned downstream of the anolyte inlet relative to the direction of the gas flow.
In one embodiment, the single scrubbing tower comprises a single scrubbing liquid outlet upstream of the anolyte inlet.
One embodiment provides a system, wherein the single scrubbing tower comprises a scrubbing liquid outlet between the catholyte inlet and the anolyte inlet, and a further scrubbing liquid outlet upstream of the anolyte inlet.
One embodiment of the disclosure provides a system comprising a first scrubbing element and a second scrubbing element, and wherein the direction of the gas flow is from the first scrubbing element to the second scrubbing element.
In one embodiment of the disclosure, the electrolysis element consumes 4.0 to 9.0 A per g sulfur per hour. In one embodiment, the electrolysis element consumes 4.0 to 4.2 A per g sulfur per hour, 4.2 to 4.4 A per g sulfur per hour, 4.4 to 4.6 A per g sulfur per hour, 4.6 to 4.8 A per g sulfur per hour, 4.8. to 5.0 A per g sulfur per hour, 5.0 to 5.2 A per g sulfur per hour, 5.2 to 5.4 A per g sulfur per hour, 5.4 to 5.6 A per g sulfur per hour, 5.6 to 5.8 A per g sulfur per hour, 5.8 to 6.0 A per g sulfur per hour, 6.0 to 6.2 A per g sulfur per hour, 6.2 to 6.4 A per g sulfur per hour, 6.4 to 6.6 A per g sulfur per hour, 6.6 to 6.8 A per g sulfur per hour, 6.8 to 7.0 A per g sulfur per hour, 7.0 to 7.2 A per g sulfur per hour, 7.2 to 7.4 A per g sulfur per hour, 7.4 to 7.6 A per g sulfur per hour, 7.6 to 7.8 A per g sulfur per hour, 7.8 to 8.0 A per g sulfur per hour, 8.0 to 8.2 A per g sulfur per hour, 8.2 to 8.4 A per g sulfur per hour, 8.4 to 8.6 A per g sulfur per hour, 8.6 to 8.8 A per g sulfur per hour, and/or 8.8 to 9.0 A per g sulfur per hour. In one embodiment, the electrolysis element consumes 5.0 to 7.4 A per g sulfur per hour, such as 5.2 to 7.2 A per g sulfur per hour, such as 5.4 to 7.0 A per g sulfur per hour, such as 5.6 to 6.8 A per g sulfur per hour, such as 5.8 to 6.6 A per g sulfur per hour, such as 6.0 to 6.4 A per g sulfur per hour, such as about 6.2 or 6.3 A per g sulfur per hour. In one embodiment, the electrolysis element is configured to consume 4.0 to 9.0 A per g sulfur per hour. In one embodiment, the electrolysis element is configured to consume 4.0 to 4.2 A per g sulfur per hour, 4.2 to 4.4 A per g sulfur per hour, 4.4 to 4.6 A per g sulfur per hour, 4.6 to 4.8 A per g sulfur per hour, 4.8. to 5.0 A per g sulfur per hour, 5.0 to 5.2 A per g sulfur per hour, 5.2 to 5.4 A per g sulfur per hour, 5.4 to 5.6 A per g sulfur per hour, 5.6 to 5.8 A per g sulfur per hour, 5.8 to 6.0 A per g sulfur per hour, 6.0 to 6.2 A per g sulfur per hour, 6.2 to 6.4 A per g sulfur per hour, 6.4 to 6.6 A per g sulfur per hour, 6.6 to 6.8 A per g sulfur per hour, 6.8 to 7.0 A per g sulfur per hour, 7.0 to 7.2 A per g sulfur per hour, 7.2 to 7.4 A per g sulfur per hour, 7.4 to 7.6 A per g sulfur per hour, 7.6 to 7.8 A per g sulfur per hour, 7.8 to 8.0 A per g sulfur per hour, 8.0 to 8.2 A per g sulfur per hour, 8.2 to 8.4 A per g sulfur per hour, 8.4 to 8.6 A per g sulfur per hour, 8.6 to 8.8 A per g sulfur per hour, and/or 8.8 to 9.0 A per g sulfur per hour. In one embodiment, the electrolysis element is configured to consume 5.0 to 7.4 A per g sulfur per hour, such as 5.2 to 7.2 A per g sulfur per hour, such as 5.4 to 7.0 A per g sulfur per hour, such as 5.6 to 6.8 A per g sulfur per hour, such as 5.8 to 6.6 A per g sulfur per hour, such as 6.0 to 6.4 A per g sulfur per hour, such as about 6.2 or 6.3 A per g sulfur per hour. The consumption is based on an electrolysis element having an efficiency of about 25%. The amount of current consumed can be further affected if the electrolysis element performs with an efficiency different from 25%, i.e. the current upwards can be adjusted upwards if the electrolysis element performs with an efficiency lower than 25%, or the current can be adjusted downwards if the electrolysis element performs with an efficiency higher than 25%. In one embodiment, such modification is inversely proportional to the performance of the electrolysis element.
In one embodiment of the disclosure, the electrolysis element is an electrochemical cell.
In one embodiment of the disclosure, the system comprises one or more filters. In one embodiment, the filter is positioned after the liquid outlet to a wet scrubbing element, such as after the wet scrubbing element to which the anolyte is supplied. In one embodiment of the disclosure, the filter is positioned at or after the liquid outlet of the one or more wet scrubbing elements.
In one embodiment of the disclosure, the system comprises one or more pumps, such as:
In one embodiment, the system comprises a filter. In one embodiment, the filter is capable of separating solids from liquid. In one embodiment, the filter comprises a filter medium through which fluids can pass, but wherein solids are retained. In one embodiment the filter is a membrane filter. In one embodiment, the filter is capable of removing ions, such as specific ions, from the liquid phase. In one embodiment, the filter is an ion chromatograph.
In one embodiment of the disclosure, the system comprises one or more filters, such as
In one embodiment of the present disclosure, the system comprises one or more flow control valves. In one embodiment, the flow rate of a liquid or a gas may be controlled by such flow control valve. In one embodiment, the flow rate of a liquid or a gas may be controlled by a pump.
One embodiment of the present disclosure provides for a fuel gas processing plant comprising the system as disclosed herein.
One embodiment of the disclosure provides for a system configured for performing the method as disclosed herein.
On embodiment provides for a method for desulfurisation of gas, said method comprising the steps of
In one embodiment, step vii. further comprises a step of:
In one embodiment of the disclosure, the content of H2S in the gas comprising the sulfur compound is 10 to 20.000, such as 10 to 5000 ppm, such as 100 to 4000 ppm, such as 500 to 2500 ppm. In one embodiment of the disclosure, the content of H2S in the gas comprising the sulfur compound is 20 to 250 ppm, such as 50 to 250 ppm.
In one embodiment of the disclosure, the content of H2S in the gas comprising the sulfur compound varies substantially between feedstock compositions and/or other external parameters, such as temperature.
In one embodiment, the variation in H2S content is of a type such that a method comprising no introduction of catholyte would be insufficient to ensure removal of H2S without introducing Cl2 to the gas.
In one embodiment, the variation in H2S content is of a type such that a method comprising no introduction of catholyte would be insufficient to ensure removal of H2S without introducing Cl2 to the gas unless the current applied to the electrolysis element was continuously modified to accommodate the varying content of H2S.
In one embodiment, the method disclosed herein can tolerate a 100% variation in the content of H2S in the gas comprising sulfur compounds while still removing substantially all H2S from the gas and without introducing substantially any C2 to the gas.
In one embodiment, the method disclosed herein can tolerate a 50% variation in the content of H2S in the gas comprising sulfur compounds while still removing substantially all H2S from the gas and without introducing substantially any C2 to the gas, and without varying the current applied to the electrolysis element.
In one embodiment, no adjustment of the voltage and/or current supplied to electrolysis element is required to accommodate a 100% variation of H2S content in the gas.
In one embodiment of the disclosure, the alkali chloride is NaCl.
In one embodiment of the disclosure, the scrubbing liquid comprises between 1 and 300 g/L NaCl, such as between 50 and 250, such as between 180 and 220, such as between 200 and 300 g/L.
In one embodiment of the present disclosure, the method does not comprise a step of adding NaOH, NaClO, HClO, or Cl2 from an external source to the scrubbing liquid. In one embodiment of the present disclosure, the method comprises generation of NaOH, NaClO, HClO, and Cl2, such as electrochemical generation.
One embodiment of the present disclosure provides for a method of desulfurising gas, said method using the system disclosed herein.
Set-up with bypass: power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, scrubber Ø110 mm, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 2 pumps 10-50 L/min and 1-5 L/min. A schematic of the setup used is shown in
The assessment was conducted at using a current of 0-90 A and a voltage of 3-13 V. A total liquid volume of 27 L was circulated in the system having an initial NaCl concentration of 300 g/L for the set-up without the bypass. Without bypass of the electrochemical cell, the first pump, supplying the scrubber directly, was run with a flow rate of 12.5-13 L/min.
The assessment was conducted at using a current of 0-4.5 A and a voltage of 0-12 V. A total liquid volume of 7 L was circulated in the system having an initial NaCl concentration of 50 g/L for the set-up with the bypass
With bypass of the electrochemical cell, the first pump, was run with a flow rate of 5-500 L/min. The second pump, was run with a flow rate of 0.5-1 L/min.
Running the setup without bypass of the electrochemical provided Faraday efficiency of 6 to 19%. Bypass of the electrochemical cell increased the Faraday efficiency of electrochemical cell to between 23 and 42%. These findings support that the presence of a bypass improves efficiency of the system.
Separately controlled flow in the electrochemical cell allows for improved Faraday efficiency of the electrochemical cell.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, 1 scrubber Ø110, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 2 pumps 10-50 L/min and 1-5 L/min.
The assessment was conducted at using a current of 0.5-3.9 A and a voltage of 3.3-8.4 V. A total liquid volume of 7 L was circulated in the system. Inlet concentration of H2S: 1000 ppm, pump flow 500 L/h, initial NaCl concentration in liquid 50 g/L. The first pump, supplying the scrubber directly, was run with a flow rate of 500 L/h. The second pump, supplying the electrochemical cell was run with a flow rate of 1 L/min. A schematic of the setup used is shown in
When the gas flow increases a higher amount of current was needed to remove the H2S. Total gas flows of 150 g/h, 225 g/h, 300 g/h and 450 g/h was tested and removal of >98.6% of the H2S was achieved for all flows. The current as a function of gas flow is shown in
H2S was removed at different gas flows. These findings demonstrate that the system of the disclosure provides a robust platform for the removal of H2S from gas, capable of accepting a wide range of gas flows.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, scrubber Ø110, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 2 pumps 10-50 L/min and 1-5 L/min.
The assessment was conducted at using a voltage of 3.5-4.3 V. A total liquid volume of 7 L was circulated in the system. Gas flow 300 g/h, inlet concentration of H2S: 500 ppm, pump flow 500 L/h, initial NaCl concentration in liquid 50 g/L. The first pump, supplying the scrubber directly, was run with a flow rate of 500 L/h. The second pump, supplying the electrochemical cell was run with a flow rate of 1 L/min. A schematic of the setup used is shown in
When a current of 0.8 A was applied to the electrochemical cell, 12.4 ppm H2S was left in the purified gas, corresponding to removal efficiency of 97.5%. When a current a 1.2 A was applied to the electrochemical cell, 2.8 ppm H2S was left in the purified gas, corresponding to removal efficiency of 99.4%.
The system was capable of removing H2S down to very low concentration, provided a sufficient current is applied. For this specific example, the removal of H2S improved significantly upon increasing the current from 0.8 to 1.2 A. However, the employed current should not be taken as an absolute threshold, as the current required depends on the size of the electrochemical cell, which in turn depends on the capacity of the system.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, scrubber Ø110, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 2 pumps 10-50 L/min and 1-5 L/min.
Gas flow 450 g/h, inlet concentration of H2S: 500 ppm, initial NaCl concentration in liquid 50 g/L, current 1.6 A. The first pump, supplying the scrubber directly, was run with a flow rate of 50-500 L/h. The second pump, supplying the electrochemical cell was run with a flow rate of 1 L/min. A total liquid volume of 7 L was circulated in the system. A schematic of the setup used is shown in
The total solvent flow was tested at 50 L/h, 100 L/h, 150 L/h, 250 L/h and 500 L/h. The H2S concentration in the cleaned gas was between 5 and 8 ppm for all set points. The H2S content as a function of the solvent flow is shown in
It was found that the system is capable of removing H2S essentially independent of solvent flow rate. These findings demonstrate that the system of the disclosure provides a robust platform for the removal of H2S from gas, capable of accepting a wide range of gas flows and providing consistent removal of H2S.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, two scrubbers Ø110, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 2 pumps 10-50 L/min and 1-5 L/min.
Gas flow 225 g/h, Inlet concentrations of H2S: 800 and 1000 ppm, initial NaCl concentration in liquid 50 g/L, current 1.8 A. The first pump, supplying the scrubber directly, was run with a flow rate of 500 L/h. The second pump, supplying the electrochemical cell was run with a flow rate of 1 L/min. A total liquid volume of 6.66 L was circulated in the scrubber 1 system. A total liquid volume of 7.2 L was circulated in the scrubber 2 system. A schematic of the setup used is shown in
Using a current of 1.8 A, the system removed H2S from 1000 ppm down to 5-7 ppm, with no chlorine present in the desulfurised gas. When the inlet concentration of H2S was reduced to 800 ppm, the electrochemical cell was found to produce excess Cl2 gas relative to the amount of H2S present in the gas: the content of Cl2 gas was measured to reach a concentration of 400 ppm in the desulfurized gas. The results are shown in
The results above suggest that employing an excessive amount of current relative to the H2S present in the inlet gas can lead to a build-up of C2 in the purified gas. However, the employed currents should not be taken as absolute thresholds, as the current needed will depend on the size of the electrochemical cell, which in turn depends on the capacity of the system.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, 2 scrubbers Ø110, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 3 pumps 10-50 L/min, 10-50 L/min and 1-5 L/min.
Gas flow 225 g/h, inlet concentration of H2S: 800 ppm, initial NaCl concentration in liquid 50 g/L, current 2 A. The first pump supplying scrubber 1 directly, was run with a flow rate of 500 L/h. The second pump supplying the electrochemical cell was run with a flow rate of 1 L/min. The third pump supplying scrubber 2 was run with a flow rate of 8 L/min. A total liquid volume of 6.66 L was circulated in the scrubber 1 system. A total liquid volume of 7.2 L was circulated in the scrubber 2 system. A schematic of the setup used is shown in
Using a current of 2 A, the system removed 800 ppm H2S and the electrochemical cell produced excess Cl2 gas. The Cl2 gas was measured to reach a concentration of 400 ppm in the desulfurized gas. A secondary scrubber with tap water was used to remove the Cl2 gas. The content of Cl2 in the scrubber 1 outlet gas and the scrubber 2 outlet gas is shown in
A high current was applied to the electrochemical cell in order to induce a transfer of chlorine to the desulfurized gas. This chlorine was successfully removed with tap water, but said water had only moderate capacity for chlorine before becoming saturated. These findings indicates another scrubbing liquid should be employed in order to facilitate recycling of the scrubbing liquid.
Power supply from 0-12 V, 0-60 A, electrochemical cell 10 cm2 electrode areas, membrane proton exchange, 2 scrubbers Ø110 mm, height 60 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm, 3 pumps 10-50 L/min, 10-50 L/min and 1-5 L/min.
Gas flow 225 g/h, inlet concentration of H2S: 800 ppm, initial NaCl concentration in liquid 50 g/L, current 1.8 A, solvent flow: 500 L/h. The first pump supplying scrubber 1 directly, was run with a flow rate of 500 L/h. The second pump supplying the electrochemical cell was run with a flow rate of 1 L/min. The third pump supplying scrubber 2 was run with a flow rate of 8 L/min. A total liquid volume of 6.66 L was circulated in the scrubber 1 system. A total liquid volume of 7.2 L was circulated in the scrubber 2 system. A schematic of the setup used is shown in
Using a current of 1.8 A, the system removed 800 ppm H2S and the electrochemical cell produced excess Cl2 gas. The Cl2 gas was measured to reach a concentration of 400 ppm in the cleaned gas. A secondary scrubber with tap water was used to remove the Cl2 gas. NaOH (s) was added to the solvent in the secondary scrubber. The secondary scrubber was capable of removing Cl2 for more than 80 hours.
A deliberate high current compared to H2S flow was applied to the electrochemical cell in order to induce a transfer for chlorine to the desulfurized gas. This chlorine was successfully removed with tap water having been made basic with sodium hydroxide pellets. The introduction of sodium hydroxide to the water provided a higher capacity for removing chlorine compared to tap water. However, the liquid still had a finite capacity for removing Cl2 before becoming saturated. These findings indicate the benefits of using alkaline, such as hydroxide ions, to remove Cl2 from gas. These findings strongly indicate the benefits of generating aqueous alkali hydroxide for continuous scrubbing of Cl2. Electrochemical generation of alkali hydroxide would eliminate the requirement of maintaining the system with regular refills of alkali hydroxide.
Based on the findings of examples 6 and 7, it is contemplated that such as setup is capable of efficiently desulfurize the gas while simultaneously keeping the content of Cl2 in the purified gas low.
Based on the findings of examples 6 and 7, it is contemplated that such as setup is capable of efficiently desulfurize the gas while simultaneously keeping the content of Cl2 in the purified gas low.
The scrubbers may for example be positioned side by side, or they may be stacked, such as having the second scrubber stacked on top of the first scrubber.
Based on the findings of examples 6 and 7, it is contemplated that such as setup is capable of efficiently desulfurize the gas while simultaneously keeping the content of Cl2 in the purified gas low.
Based on the findings of examples 6 and 7, it is contemplated that such as setup is capable of efficiently desulfurize the gas while simultaneously keeping the content of Cl2 in the purified gas low.
A process flow diagram of the system can be seen in
During operation, electrical current was adjusted in order to achieve steady state conditions between 1-20 ppm H2S in the outlet gas of the system. Several H2S measurements were made at each steady state to ensure representative data.
The scrubber column was filled with randomly stacked pall rings made from PVC. The rings has a surface area of 340 m2/m3 and a void fraction of 87%.
pH, temperature and redox measurement sensors from Bürkert were placed in the liquid flow before and after the scrubber unit, as well as on the inlet flow to the electrochemical cell, and in the outlet flow from each of the chambers of the electrochemical cell (AP1-4 in
After exiting the scrubber, the cleaned biogas was analyzed (see unit D in
The gas used in the experiments was a synthetic biogas consisting of H2S, N2 and CO2. CH4 is a main component of biogas, but during the initial setup and testing of the setup, it was found that the CH4 in the gas phase is inert during the process. It was therefore replaced with an equal volume of nitrogen due to considerations of cost and safety. The flow of each of the component gasses was controlled by a Bronkhorst miniCori Coriolis flow controller (model M13V10I) in order to ensure accurate measurements. The gasses were mixed before entering the scrubber unit.
A titanium oxide alloy was used for the electrodes. The chambers of the electrochemical cell were divided by a Nafion membrane, which allows water and cations to move through the membrane, but not anions. This ensured that the active chlorine was kept on the anode side of the cell. The liquid flow through the cell was kept high for all experiments as to reduce or eliminate influence by limitations in diffusion speed.
The flow of solvent through the scrubber unit was controlled by a Grundfoss membrane pump, which made it possible to adjust the solvent flow with a high degree of accuracy. The solvent flow through the electrochemical cell was achieved by using a smaller centrifugal pump. It was not possible to adjust the solvent flow with the centrifugal pump, why the precise solvent flow through the electrochemical cell is unknown. However, it was approximately 1 L/min for all experiments. The approximate flow rate through the electrochemical cell was measured with a measuring cup and a stopwatch. This flow rate is within the optimal operation parameters given by the supplier.
To determine the contents of sulphate ions in the liquid of the scrubber, an ion chromatograph was used. This method measures the speed of the ions as they move through a charged resin. Ions with less affinity for the resin will move faster compared to ions with higher affinities. In this way the concentration of the ions can be determined by measuring the conductivity in the outlet liquid as it changes over time (D. C. Harris, Quantitative chemical analysis, 7th ed. New York N.Y.: W.H. Freeman and Co., 2007).
To examine the effect of the solvent flow through the scrubber, all process parameters were kept constant while the scrubber flow (flow 4 in
The results for the outlet H2S concentration as a function of the solvent flow through the scrubber can be seen in
The same amount of chlorine is needed for removing the H2S, regardless of the solvent flow rate. It can therefore be assumed, that the concentration of chlorine in the solvent rises proportionally with the decrease in solvent flow rates. The concentration of chlorine at 50 L/h is therefore 10 times higher than the concentration at 500 L/h.
The removal efficiency can be adjusted by changing the amount of electrical current through the electrochemical cell. At a high current, the amount of chlorine produced will increase and more H2S will be oxidized. At a low current, less H2S will be oxidized since less chlorine is available for reaction.
The removal efficiency in the conducted experiment was purposefully set to be slightly below 1. Using the definition of current efficiency (equation below), the efficiency of the system is found to be approximately 0.26 for all solvent flow rates.
Where NH2S is the amount of moles of H2S removed per second, NA is Avogadro's number, I is the current running through the electrochemical cell, and C is Coulombs number.
The setup was as described in Example 12.
Several gas flows and H2S concentrations were tested in order to examine the effect of the gas flow on the scrubber system. The electrical current flowing through the electrochemical cell was adjusted, in order to achieve an outlet concentration between 1-20 ppm H2S. The steady state values achieved during the experiments can be seen in Table 3 (C2.1-C2.9).
In
The removal efficiency is 99%±1% for all steady state points. Constant removal efficiency was achieved by tuning the applied current to the electrochemical cell. From
The influence of H2S concentration on process performance can also be examined by calculating the current efficiency. This is indicated in
In
The setup of Example 12 was used.
To examine the long term stability of the system, a test of the laboratory setup was run for 30 hours. During this period the solvent flow, inlet gas flow, and H2S concentrations were all kept stable. The steady state process parameters can be seen in Table 3 (C3.1). The results for the outlet H2S concentration, as well as the current applied to the electrochemical cell, can be seen in
The system is seen to be stable at constant applied current with H2S outlet concentrations deviating only up to 2 ppm during more than 20 hours of continuous operation. This deviation is less than 0.5% of the inlet concentration. During the entire experiment, the mean current efficiency of the process was calculated to be approximately 21%. During operation, pH decreased gradually from 8 to 0.5 during the initial 3 hours of the experiment. This decrease in pH is caused mainly by sulfuric acid formed by the absorption and subsequent oxidation of H2S and sulfur. Absorption of CO2 into the solvent will only play a minor role in the pH drop, since CO2 is not captured at low pH values.
The setup of Example 12 was used.
To determine the cause of the efficiency loss, an analysis of the liquid phase in the scrubber system was conducted. During the long term experiment, several liquid samples were extracted periodically. This was done to determine whether the elemental sulfur reacted with active chlorine to form sulphate. The sulphate content of the liquid samples was measured using an ion chromatograph. The oxidation from sulfur to sulphate when reacting with hypochlorous acid is:
The sulphate concentration for the extracted liquid samples compared to the total amount of H2S captured during the experiment, can be seen in
The total amount of H2S captured is represented by the dark grey line and increases almost completely linearly during operation. The linear progression is caused by both the inlet gas flow and capture rate being quite stable during the prolonged operation as seen in
The amount of sulphate measured in the liquid samples is represented by the light grey line in
Oxidation of sulfur to sulphate is seen to use three times as much active chlorine as the reaction from H2S to sulfur. Therefore, this reaction constitutes a considerable amount of the electrical current consumed in the cleaning process. In the long term experiment, the reaction from sulfur to sulphate consumed approximately 54% of the total current applied to the system. The oxidation of H2S to sulfur consumed only 21%, leaving 25% currently unaccounted for. That a majority of the efficiency loss comes from formation of sulphate fits well with the observation that a large concentration of active chlorine leads to lower efficiency. A large concentration of chlorine may increase the reaction rate of unwanted sulfur oxidation, and thus lead to formation of additional sulphate and a loss of oxidant.
In the setup of Example 2, Faraday efficiency was assessed.
A process flow diagram of the set-up is presented in
In experiment A, the gas-gas reaction of C2 and H2S is observed. Results from the experiment is presented in
In experiment B, the effect of changing the applied current was investigated. In
From experiment B, it can be observed that when changing the applied current, the removal of hydrogen sulfide also changes. Specifically, it can be observed that there is a point where the development of hydrogen sulfide removal and ORP value of the solvent changes direction. Furthermore, it can be observed that the changes to the ORP value and the hydrogen sulfide concentration is not independent on the conditions of the solvent. The ORP value and hydrogen sulfide concentration changes much more slowly after the change in current at 11:15 than before.
Solid sulfur was observed to form inside the scrubber during experiments A and B as precipitates deposited on the inner surface of the scrubber. Following the experiments, samples of the solid sulfur was collected and analysed using a scanning electrode microscope (SEM) equipped with energy dispersive x-ray spectroscopy (EDS).
The solid samples consisted of small particles. The sample consisted of 93% sulfur with some sodium (4%) and chlorine (3%). The sodium and chlorine are most likely traces of the solvent found in the sulfur. The sample was prepared on carbon tape to ensure conductivity, and the carbon content of the sample has therefore been subtracted. Carbon is not expected to be found in the solid sulfur sample.
In conclusion, it is possible to remove hydrogen sulfide from a gas using only chlorine gas. The chlorine gas in these experiments were emitted from a low pH-value solvent containing high concentrations of active chlorine. The active chlorine was generated in an electrochemical cell. The active chlorine and hydrogen sulfide reacted inside a scrubber where the packing had been removed.
The results were confirmed in a series of experiments, and through analysis of a series of values. The behaviour could be observed both from the hydrogen sulfide concentration and through the oxidation reduction potential of the solvent.
The results show that a significant period of time is required for the system to stabilize. Furthermore, solid sulfur is observed to form at the sides of the scrubber. This results was confirmed through analysis of solid samples collected from the scrubber. The samples were analysed with a scanning electrode microscope equipped with energy dispersive x-ray spectroscopy. The solid was found to have a sulfur concentration of 93% with traces of sodium chloride consisting of the remaining 7%.
Set-up: power supply from 0-12 V, 0-300 A, electrochemical cell 0.16 m2 electrode areas, membrane proton exchange, scrubber 0280 mm, height 100 cm, full-cone spray nozzle, random packing elements Raschig Pall rings 15 mm×15 mm,
4 pumps were used: Anode flow of 320-1020 L/h, another pump for the cathode flow of 60-780 L/h, another for scrubber 1 with a flow of 0-1440 L/h and the last for scrubber 2 with a flow of 270-690 L/h.
The split configuration were used, there the anode flow of the electrochemical cell were used in scrubber 1 and the cathode flow were used in scrubber 2.
The assessment was conducted at using a current of 10-90 A and a voltage of 2.7-3.6 V. A total liquid volume of 12 L was circulated in the system having an initial NaCl concentration of 100 g/L. The gas flow was varied from 6-13.4 Nm3/h. The H2S concentration varied in the biogas between 866-1633 ppm. Removal down to 0 ppm was achieved.
The process has been showed to remove H2S from raw biogas in different settings.
The result include process parameters that can easily be scaled up.
The results include a recreation of the gas-gas reaction showed in the laboratory.
| Number | Date | Country | Kind |
|---|---|---|---|
| 21190147.5 | Aug 2021 | EP | regional |
| 22177586.9 | Jun 2022 | EP | regional |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/EP2022/072258 | 8/8/2022 | WO |
