Patent Application
20230113771
This invention relates to a method and process plant for treatment of a stream of mixed compounds obtained from a process comprising decomposition and/or conversion of a wood or pulp material.
There is an increasing interest in bio-based chemicals, fuels and materials and thereby also an interest in increasing efficiency and flexibility of methods and process plants using bio-material as raw material. An example in this field of technology is disclosed in SE539579C2 where raw methanol obtained as a by-product in the kraft or sulfate process of pulp production in a pulp mill is purified by removing e.g. sulphurous compounds. The purified methanol may then be used as a non-fossil fuel or as a component in other processes.
An object of this invention is to provide an improved method and process plant for handling and utilizing a stream of bio-based raw material, such as the raw methanol used as raw material in SE539579C2. This object is achieved by the method and process plant defined by the technical features contained in the corresponding independent claims. The dependent claims contain advantageous embodiments, further developments and variants of the invention.
The invention concerns a method for treatment of a stream of mixed compounds obtained from a process comprising decomposition and/or conversion of a wood or pulp material, the method comprising: feeding the stream through a processing arrangement comprising one or more treatment units arranged to separate at least a first compound from other compounds in the stream and form a first product flow containing the first compound, wherein the one or more treatment units comprises at least a first primary separation unit arranged to separate one or more compounds other than the first compound from the stream.
The method further comprising: feeding the compounds separated from the first compound in the first primary separation unit to a first auxiliary separation unit so as to separate a second compound from at least one of the other compounds separated from the first compound in the first primary separation unit and thereby increase the purity of said second compound and form a second product flow in the form of a purified second compound and/or a purified derivative of the second compound, wherein the second compound is dimethyl sulfide (DMS, CH3—S—CH3), methyl mercaptan (CH3—S—H) or acetone (CH3—CO—CH3).
The method of this disclosure thus produces other compounds, such as DMS, DMSO (dimethyl sulfoxide, oxidized derivative of DMS) and/or acetone, as a complement or alternative to the first compound, that may be methanol. This allows for a selection of which product compound(s) to focus on when operating the method, i.e. the method allows for optimizing production (or purity) with regard to the selected product compound(s). As a result, the method becomes flexible and efficient. For example, if the demand for purified DMS increases, the method can be operated to increase production of DMS while decreasing production of methanol. As will be further described below, the method of this disclosure also provides for increased flexibility and efficiency by the use of additional compound flows within the process arrangement or flows fed into the processing arrangement from an adjacent paper mill. For instance, sulphur compounds (or sulfur compounds, both spellings are used in this disclosure) separated in the processing arrangement, such as H2S, may be used to convert methanol to DMS in a recirculation arrangement or produce additional DMS by reaction with lignin obtained from black liquor treatment of wood material.
The method of the present disclosure is in contrast to e.g. SE539579 where the focus is set only on purifying methanol and where no particular attention is paid to several of the compounds removed from the raw methanol, such as the volatile compounds and acetone. As explained in more detail below, the present method may produce purified methanol as one of the purified products but may alternatively be operated without any purpose of purifying methanol and instead even use methanol as a raw material for producing other compounds. If the first compound is methanol, the first product flow containing the first compound may in such a case have a relatively low mass flow rate and a low purity of the first compound. Such a product flow may be used for combustion and providing heat to e.g. the processing arrangement. The first compound may be another compound than methanol.
In the method of this disclosure, the first compound may be stepwise purified when the raw material stream is fed through the processing arrangement (which may be denoted “biorefinery”). Similar treatment units as used in SE539579, such as the distillation units, may be used also in the method described here. However, the type(s) and number of treatment units required for the present method depends on the particular application.
The first primary separation unit defined above (which is named “first” just to specify a separation unit that forms part of the processing arrangement, not necessarily because it has a certain position in a series of separation units) is typically a distillation unit or stripper but may instead be configured for membrane-filtering or other separation. The separation unit handling the raw material stream is here denoted primary separation unit to distinguish from the auxiliary separation unit. The second compound separated in the first auxiliary separation unit may be a volatile evaporated fraction or a liquid fraction from a condenser-type of auxiliary separation unit. As will be described further below, the process arrangement preferably comprises also a second primary separation unit and a corresponding second auxiliary separation unit so as to allow separation of a third purified compound, such as acetone, in addition to the second compound, such as DMS, that in such a case may be separated and purified at the first (primary) separation unit upstream of the second (primary) separation unit. The auxiliary separation units do not handle the raw material stream but only the compounds separated from that stream in the corresponding primary separation unit.
As to the term “purified”, e.g. “purified second compound”, this generally means sufficiently purified for the intended purpose. As is well known in the field, a chemical compound is never 100% pure and increasing purity is almost always connected to an increasing cost. If “purified methanol” is to be produced, e.g. as a purified first compound in the first product flow, the purity may be >90, >95, >99, >99.5, >99.85 or >99.9 weight %. For DMS, methyl mercaptan and acetone, the purity of the “purified compound” typically may be >90, >95. >99 or >99.9 weight %. The process arrangement can be adapted to reach certain degrees of product purity, for instance by including additional auxiliary separation units and/or recirculating selected flows. The process arrangement may also be operated in different ways to reach certain degrees of product purity, the temperature in a certain separation unit may for instance be increased or decreased.
The term “product flow” indicates an outgoing flow from a treatment unit and thus a flow of some kind of product formed in the process. But it is not necessarily so that a product flow, in particular not the first product flow, contains only one purified compound product that is taken out from the processing arrangement or the process plant where the processing arrangement is located. A product flow may be used as an incoming flow at some other point in the process plant. If methanol is the first compound it may be that its purity is low in the first product flow, in particular if it is used in the process as a reactant for producing additional amounts of DMS, and if so the first product flow may be used as a fuel product.
In an embodiment the one or more treatment units further comprises a second primary separation unit arranged to separate at least the first compound from other compounds in the stream, wherein the method comprises: feeding the compounds separated from the first compound in the second primary separation unit to a second auxiliary separation unit so as to separate a third compound from at least one of the other compounds separated from the first compound in the second primary separation unit and thereby increase the purity of said third compound and form a third product flow in the form of a purified third compound or a purified derivative of the third compound, wherein the third compound is dimethyl sulfide (DMS, CH3—S—CH3), methyl mercaptan (CH3—S—H) or acetone (CH3—CO—CH3), and wherein the second and third compounds are different compounds.
In embodiments the first and/or the primary separation unit is a distillation unit.
In an embodiment the processing arrangement comprising at least two treatment units arranged in series in relation to the flow of the stream containing the first compound.
In an embodiment the processing arrangement is arranged to be capable of purifying the first compound until it forms a first product flow in the form of a purified first compound.
In an embodiment the first primary separation unit is arranged to separate compounds from the stream that have a boiling point that is lower than that of the first compound.
In an embodiment the first auxiliary separation unit is based on deviating boiling points.
In an embodiment the second primary separation unit is arranged to separate compounds from the stream that have a boiling point that is lower than that of the first compound.
In an embodiment separation in the second auxiliary separation unit is based on deviating boiling points.
In an embodiment the first compound is methanol. In such a case the first product flow may contain methanol, ethanol and water. Further separation units may be used to increase the purity of methanol and/or ethanol if desired.
In an embodiment the second compound is dimethyl sulfide (DMS, CH3—S—CH3) or methyl mercaptan (CH3—S—H). DMS may be separated from e.g. methyl mercaptan in the first auxiliary separation unit. Another compound that may be separated from DMS in the first auxiliary separation unit is H2S. As an example, DMS is the second compound and purified DMS (or DMSO) forms the second product flow, whereas methyl mercaptan (and other compounds separated from DMS) forms a flow used at another location of the process arrangement. In another example, also purified methyl mercaptan forms a product flow, whereas H2S, purified or in a mix with some other compounds, forms a (product) flow used at another location of the process arrangement.
In an embodiment the third compound is acetone (CH3—CO—CH3).
In an embodiment where the second compound is dimethyl sulfide (DMS, CH3—S—CH3) or methyl mercaptan (CH3—S—H), the third compound is acetone (CH3—CO—CH3). Typical acetone impurities, such as methanol and volatile sulphur compounds, may be separated and removed from acetone in the second auxiliary separation unit. An additional auxiliary separation unit may be included to, for instance, remove methanol from acetone in the second auxiliary separation unit and remove more volatile impurities in the additional auxiliary separation unit.
In an embodiment the first primary separation unit is arranged upstream of the second primary separation unit in relation to the flow of the stream containing the first compound.
In an embodiment the method comprises: operating the processing arrangement so as to increase a mass flow rate of the second compound in the second product flow while decreasing a mass flow rate of the first compound in the first product flow.
This can be done by e.g. changing temperature or pressure in the first primary separation unit so that a larger fraction of the second compound is separated from the stream containing the first compound. This generally also results in that a larger fraction of the first compound follows the second compound in the separation. This accompanying first compound can be removed in an auxiliary separation unit if desired to increase purity of the second compound. In effect this typically leads to a reduced total amount of the first compound in the outgoing stream from the first primary separation unit and thereby to a reduced amount/concentration of the first compound in the first product flow. Similar can be said for the third compound and the second primary separation unit. Some of the first compound, such as methanol, can thus be spent on producing more of the second product, such as DMS or acetone, when so desired.
Another way of allowing increased production of the second (or third) compound is to recirculate a portion of the stream containing the first compound so as to pass it through a primary separation unit an additional time.
In an embodiment the method comprises: recirculating a portion of the stream in a recirculation flow line from a point in the processing arrangement downstream of a separation unit where DMS and/or methyl mercaptan is separated from the stream, to a point in the processing arrangement upstream of the separation unit where DMS and/or methyl mercaptan is separated from the stream, wherein the recirculated portion of the stream during recirculation is fed through a DMS/methyl mercaptan production reactor to which is fed, via a supply line, one or more sulphur compounds capable of reacting with the first compound or another compound in stream so as to form DMS and/or methyl mercaptan.
In such an embodiment the production of DMS/methyl mercaptan can be increased by increasing the portion of the stream that is recirculated. The downstream point where the recirculation of the stream starts can in principle be anywhere downstream the separation unit in question, i.e. directly downstream that separation unit or downstream one or more further treatment units. As methanol is converted to DMS or methyl mercaptan in the production reactor, the production of methanol will at the same time decrease. The composition of the sulphur compounds and the mass flow rate of the sulphur compounds fed to the production reactor may be varied depending on desired outcome of products from the process arrangement. Relative production of DMS versus methyl mercaptan depends e.g. on the amounts of H2S fed to the reactor. The sulphur compounds used for this reaction may include H2S, and these sulphur compounds may be compounds that were present in the incoming raw material stream and now can be obtained from one or more of the treatment units of the process arrangement. Alternatively, or as a complement, these sulphur compounds may be supplied from outside of the process arrangement (e.g. from some other part of an integrated plant).
In an embodiment wherein the second compound is DMS, the method comprises: feeding purified DMS from the first auxiliary separation unit to an oxidizing unit so as to oxidize DMS and form a purified derivative of DMS in the form of dimethyl sulfoxide (DMSO).
In an embodiment the method comprises: feeding a flow containing DMS and/or methyl mercaptan from a lignin treatment arrangement to a point in the processing arrangement upstream of a separation unit where DMS and/or methyl mercaptan is separated from the stream, wherein the lignin treatment arrangement is arranged to react at least a portion of a flow of incoming lignin obtained from a wood or pulp decomposition and/or conversion process with sulphur from an incoming flow of sulphur compounds so as to form DMS and/or methyl mercaptan.
This is a particularly suitable embodiment when the plant is an integrated plant comprising both the processing arrangement, i.e. the bio-refinery, as well as a pulp production process including a “wood or pulp decomposition and/or conversion process” where wood material typically is digested in black liquor. This forms an additional way of increasing the production of DMS (as well as reactive lignin formed in the lignin treatment arrangement).
In an embodiment the stream of mixed compounds is obtained from black liquor used for digestion of wood material in pulp production in a pulp mill. In particular, the stream of mixed compounds may be a condensate from evaporation of such black liquor. Alternatively, the stream of mixed compounds may be obtained from some other decomposition of wood material in e.g. a bio-refinery.
The invention also concerns a process plant for treatment of a stream of mixed compounds obtained from a process comprising decomposition and/or conversion of a wood or pulp material, the process plant comprising: a processing arrangement comprising one or more treatment units configured to, when the stream is fed through the processing arrangement, separate at least a first compound from other compounds in the stream and form a first product flow containing the first compound, wherein the one or more treatment units comprises at least a first primary separation unit arranged to separate one or more compounds other than the first compound from the stream; the processing arrangement further comprising a first auxiliary separation unit arranged in association with the first primary separation unit so as to receive the compounds separated from the first compound in the first primary separation unit, the first auxiliary separation unit being configured to separate a second compound from at least one of the other compounds separated from the first compound in the first primary separation unit and thereby increase the purity of said second compound and form a second product flow in the form of a purified second compound and/or a purified derivative of the second compound.
In an embodiment of the process plant, the one or more treatment units further comprises a second primary separation unit arranged to separate at least the first compound from other compounds in the stream, and wherein the processing arrangement further comprising a second auxiliary separation unit arranged in association with the second primary separation unit so as to receive the compounds separated from the first compound in the second primary separation unit, the second auxiliary separation unit being configured to separate a third compound from at least one of the other compounds separated from the first compound in the second primary separation unit and thereby increase the purity of said third compound and form a third product flow in the form of a purified third compound and/or a purified derivative of the third compound.
In an embodiment of the process plant, it comprises a process configured to decompose and/or convert a wood or pulp material and form the stream of mixed compounds. In a variant the process is configured for black liquor digestion of wood material and wherein the stream of mixed compounds is obtained from the black liquor.
In an embodiment of the process plant, the processing arrangement comprises at least two treatment units arranged in series in relation to the flow of the stream containing the first compound.
In an embodiment of the process plant, the processing arrangement is arranged to be capable of purifying the first compound until it forms a first product flow in the form of a purified first compound.
In an embodiment of the process plant, the first primary separation unit is arranged to separate compounds from the stream that have a boiling point that is lower than that of the first compound.
In an embodiment of the process plant, the first auxiliary separation unit is arranged to separate compounds based on deviating boiling points.
In an embodiment of the process plant, the second primary separation unit is arranged to separate compounds from the stream that have a boiling point that is lower than that of the first compound.
In an embodiment of the process plant, the second auxiliary separation unit is arranged to separate compounds based on deviating boiling points.
In an embodiment of the process plant, the first primary separation unit is arranged upstream of the second primary separation unit.
In an embodiment of the process plant, the processing arrangement is configured to be operated so as to increase a mass flow rate of the second product flow while decreasing a mass flow rate of the first product flow.
In an embodiment of the process plant, the processing arrangement comprises: a recirculation flow line arranged to recirculate a portion of the stream from a point in the processing arrangement downstream of a primary separation unit where DMS and/or methyl mercaptan is separated from the stream, to a point in the processing arrangement upstream of the primary separation unit where DMS and/or methyl mercaptan is separated from the stream; a DMS/methyl mercaptan production reactor through which the portion of the stream is fed during recirculation; and a supply line for feeding one or more sulphur compounds to the DMS/methyl mercaptan production reactor, wherein the sulphur compounds are capable of reacting with the first compound or another compound in stream so as to form DMS and/or methyl mercaptan.
In an embodiment of the process plant, the processing arrangement comprises an oxidizing unit arranged downstream the first auxiliary separation unit so as to allow oxidation of the second compound and form a purified derivative of the second compound.
In an embodiment of the process plant, it comprises a lignin treatment arrangement arranged to react at least a portion of a flow of incoming lignin obtained from a wood or pulp decomposition and/or conversion process with sulphur from an incoming flow of sulphur compounds so as to form DMS and/or methyl mercaptan, wherein the process plant further comprises a flow line for feeding DMS and/or methyl mercaptan from the lignin treatment arrangement to a point in the processing arrangement upstream of a separation unit where DMS and/or methyl mercaptan is separated from the stream.
In an embodiment of the process plant, the first compound is methanol.
In an embodiment of the process plant, the second compound is dimethyl sulfide (DMS, CH3—S—CH3), methyl mercaptan (CH3—S—H) or acetone (CH3—CO—CH3).
In an embodiment of the process plant, the third compound is dimethyl sulfide (DMS, CH3—S—CH3), methyl mercaptan (CH3—S—H) or acetone (CH3—CO—CH3), and wherein the second and third compounds are different compounds.
In an embodiment of the process plant, the second compound is dimethyl sulfide (DMS, CH3—S—CH3) or methyl mercaptan (CH3—S—H) and the third compound is acetone (CH3—CO—CH3).
Aspects of the method of this disclosure may also be described according to the following points:
The raw material composition, e.g. a raw methanol composition, a black liquor being treated with an alkaline solution and/or a sulfur source, or an acetone rich material obtained from a partial or a total condenser e.g. an acetone column total condenser, comprises a number of chemical components, wherein each of said chemical components can be separated by the process according to the present invention, as described herein, by comprising said treatment step, e.g. comprising different treatment steps, and made into products, e.g. desirable products. The same products can, for example, be produced by utilizing raw methanol composition, black liquor or lignin as the raw material composition.
The raw material composition is a stream of mixed compounds obtained from a process comprising decomposition and/or conversion of a wood or pulp material.
The process enables production of one, or more, compounds according to formula (I) within a, so called, biorefinery concept, wherein the process provides further developments of the biorefinery concept, for example, regarding production of a multiple products portfolio from raw methanol, lignin and black liquor.
With a biorefinery concept, the production is maximized on the output from both a technical, sustainability and economical perspective. This results in an increased valorization, by producing a multiple product portfolio for e.g. the chemical or energy sector, rather than maximizing the volume of only one product type.
The process has currently been constructed, and in the process impurities may be removed from methanol containing stream to obtain marketable commodities by meeting international standards. This may be done through several separation steps known as such (see e.g. SE539579C2) including acidification, distillation and extraction. During one of these stages, lights may be distilled off, containing mainly hydrogen sulfide (H2S), methyl mercaptan and dimethyl sulfide (DMS) (for example, around 30% DMS). The gaseous stream can be sent to combustion for energy recovery, however, e.g. DMS has a value as a commodity and could be separated from the mixture by differences in boiling points. Apart from the initial thermal separation of, e.g. DMS, optionally, some final polishing, e.g. process steps, may be performed to reach further improved purity, including an acceptable purity. In some instances, the process, in accordance with the present invention, produces, e.g. DMS, for example, 90 weight %, or more of DMS, 95 weight %, or more of DMS, or, alternatively, 99 weight %, or more of DMS.
Another aspect is to utilize as much of a raw material as possible, by numerous processes that combined results in a maximized resource efficiency. This can be part of a sustainability strategy, since it maximizes the amount of products and minimizes the amount of low value by-products or even waste.
In embodiments of the process said raw material composition comprises, or is, a raw methanol composition and said process comprises addition of sulfuric acid, prior to said retrieval of said retrieving composition. Further, when the raw material composition comprises, or is, a raw methanol composition, the material composition consists of a number of chemical components, wherein each of said chemical components can be separated by the process by comprising said treatment step, e.g. comprising different treatment steps, and made into products, e.g. desirable products.
In further embodiments of the process said raw material composition comprises, or is, a black liquor being treated with an alkaline solution and/or a sulfur source.
In still further embodiments of the process, lignin in alkali, e.g. black liquor, may be treated with sulfur, or other sources of sulfur such as hydrogen sulfide, and methyl mercaptane, e.g. at 200-250° C., which may also render a lignin product with improved reactivity towards formaldehyde (demethylated lignin), i.e. a reactive lignin product. The demethylation of lignin gives an increased content of cathechol structures in the lignin polymer which are known to exibit higher reactivity, for instance, in reactions with formaldehyde. Said lignin product, i.e. the reactive lignin, can be isolated by any of the methods found in the literature, e.g. precipitation by adding acid which may also be combined with membrane filtration.
In further embodiments of the process said material composition and/or said raw material composition further comprises an internal source of sulfur. The sulfur source may be external such as purchased sulfur source but may also be internal. The internal source of nucleophilic sulfur compounds may be strong gases from the pulping process or from the biorefinery process itself where a source of reduced sulfur is available. The sulfur gases in kraft pulp mills are primarily burnt in order to minimize odor problems (destruction).
In still further embodiments of the process said raw material composition is a black liquor being treated with an alkaline solution.
In even further embodiments of the process, said material composition and/or said raw material composition further comprises an internal source of sulfur, wherein the internal source of sulfur may comprise H2S and CH3SH from a methanol source, e.g. a methanol factory and, optionally, also strong gases from a Kraft pulp mill scrubbed in alkali giving HS- and CH3S-.
Further, in said oxidation step, DMS may be oxidized by using an oxidizing agent to DMSO, for example, by using oxygen as an oxidizing agent, e.g. by using a gas mainly composed of oxygen an oxidizing agent, and using a catalyst, e.g., using NOx as a catalyst in a liquid phase, wherein NOx may be any one or more of NO, N2O3, NO2 and N2O4, for example a mixture of NO, N2O3, NO2 and N2O4. In a further example of said oxidation step, DMS may be oxidized with nitrogen dioxide in nitrogen gas to DMSO, and nitrogen oxide nitrogen oxide may be formed which may be reacted back to NO2 with addition of ammonia. Thus, when the compound of formula (I) is DMSO, said treatment step comprises an oxidation step wherein DMS has been oxidized.
In the description of the invention given below reference is made to the following figure, in which:
With reference to
DMS can be produced starting from a raw material composition in accordance with the present process. The process here in Example 2 may further comprise treatment of lignin in black liquor with sulfur, or with other sources of sulfur such as hydrogen sulfide, and methyl mercaptane, e.g. at 200-250° C., i.e. treatment steps of the process.
From a stripper top (for example, “Distillation” with “Volatiles″-stream in
This stream, i.e. DMS rich stream gas phase, (see “DMS” in
From an acetone column total condenser (for example, “Distillation” with “Acetone+impurities″-stream in
Thus, in Example 4 refer to “Crude methanol”, i.e. a raw material composition which is going in to the “Biorefinery” from the left, see “Biorefinery” in
Example 5 describes a process involving production of DMS (see “DMS” in
The lignin treatment (see “Lignin treatment” in
Production of DMS comprising an internal, or external, source of sulfur. Example 6 describes a process for production of DMS (see “DMS” in
The Example 6 (see
The process plant 1 comprises a processing arrangement 2, i.e. an arrangement that may be denoted “biorefinery”.
In this particular example the treatment units include a first and a second primary separation unit 20, 40. The other treatment units 10, 30 and 50 are in this example optional but are indicated as it in many cases would be suitable to include further treatment units, such as further separation units that may form further product flows and/or units for acidic treatment of the flow or similar. For the principle of this disclosure only one of the first and second primary separation units 20, 40 is required.
The stream of mixed compounds is denoted 4a when fed to the processing arrangement 2. As the stream passes the treatment units 10-50 the composition and mass flow rate of the stream typically changes since some compounds is removed, such as more volatile compounds, and some compounds may be added, such as acid. This change of the stream is indicated by the notations 4b-4f used after the treatment units 10-50. As further described below, one or more compounds including “the first compound” will generally remain in the stream 4a-4f and form an outgoing first product flow 4f. This first product flow 4f may be a flow of a (to some degree) purified first product or may be a mix of compounds that might be used for combustion and thus for heating purposes (possibly after having removed water in an additional treatment unit, if not already removed in e.g. treatment unit 50). In the example of
The first primary separation unit 20 is arranged to separate one or more compounds other than the first compound from the stream. In this example the first primary separation unit 20 is a distillation unit that separates compounds from the stream that have a lower boiling point than the first compound.
A first auxiliary separation unit 21 is arranged in association with the first primary separation unit 20 so as to receive the compounds separated from the first compound in the first primary separation unit 20. The first auxiliary separation unit 21 is configured to, based on deviating boiling points, separate a second compound from at least one of the other compounds separated from the first compound in the first primary separation unit 20. The first auxiliary separation unit 21 may thus be a cooler/condenser. As a result of the treatment in the first auxiliary separation unit 21, the purity of the second compound increases and form a second product flow 22, 23 in the form of a purified second compound and/or a purified derivative of the second compound. See further explanation below regarding different variants for the second product flow(s).
As mentioned above, the treatment units further include the second primary separation unit 40, that is located downstream of the first separation unit 20 (in relation to the stream 4a-4f) and that also is a distillation unit arranged to separate at least the first compound from other compounds in the stream based on deviating boiling points.
The processing arrangement 2 further comprises a second auxiliary separation unit 41 arranged in association with the second primary separation unit 40 so as to receive the compounds separated from the first compound in the second primary separation unit 40. The second auxiliary separation unit 41 is configured to separate, again based on deviating boiling points, a third compound from at least one of the other compounds separated from the first compound in the second primary separation unit 40. As a result, the purity of the third compound increases and it forms a third product flow 42 in the form of a purified third compound and/or a purified derivative of the third compound.
The processing arrangement 2 is further arranged to be capable of purifying the first compound until it forms the first product flow 4f in the form of a purified first compound. As explained on various places in this disclosure, it may be beneficial to produce also a purified first compound but it is not necessary that a purified first compound is produced.
In the example of
As mentioned above, the first compound in the example of
Depending on the particular design of the processing arrangement 2, flows 22, 23 and 25 can represent different compounds, and at least one of these flows is optional, as is also an oxidizer 24 arranged downstream the first auxiliary separation unit 21. In one example, flow 22 represents purified methyl mercaptan, flow 23 represents purified DMS (optionally oxidized to DMSO in oxidizer 24), and flow 25 represents some other compounds (such as H2S) separated from the stream 4b in the first primary separation unit 20. In another example flow 22 represents purified DMS, flow 23 is optional or represents purified DMSO (i.e. a portion of the DMS is fed to oxidizer 24) and flow 25 represents some other compounds, including e.g. methyl mercaptan and H2S, separated from the stream 4b in the first primary separation unit 20. The flow 25 may serve as a source of sulphur and be fed to a “sulphur source” schematically indicated in
Besides product flows of DMS, DMSO, methyl mercaptan and sulphur compounds, including variants 22 and 23 of the second product flow, the method/process plant 1 of
As an example, the second primary separation unit 40 in the form of a distillation unit may be operated at around 61-62° C. (if atmospheric pressure) to evaporate and separate acetone (boiling point 56° C.) from e.g. methanol (boiling point 64.7° C.) and ethanol (boiling point 78.4° C.). Also water will then remain in the liquid phase. Remaining volatile compounds in the stream 4d, such as DMS (boiling point 37° C.), methyl mercaptan (boiling point 6.0° C.) and H2S (boiling point -60.3° C.) follow the acetone, as also some of the methanol. Flow 43 in
The processing arrangement 2 is further configured to be operated so as to increase a mass flow rate of the second and/or third product flow while decreasing a mass flow rate of the first product flow. This can, for instance, be done by adjusting temperature/pressure of the first and/or second primary separation units 20, 40 so that a larger fraction of the incoming stream 4b, 4d is separated and fed to the corresponding auxiliary separation unit 21, 41. By operating the auxiliary separation units 21, 41 properly, and possibly by adding further separation units, this provides for the possibility to generate a larger mass flow rate of purified DMS (and/or DMSO/metyl mercaptan) and purified acetone, while the mass flow rate of purified methanol decreases (since some methanol will be removed from the main stream 4). The method may focus completely on the output of purified second and/or third compound and no purified methanol needs to be produced.
As shown in
As seen in
This way additional amounts of DMS or methyl mercaptan are produced from methanol and sulphur compounds and introduced in the stream 4b upstream of the first primary separation unit 20. The sulphur compounds are preferably obtained at least partly from flow 25 and/or flow 43 as mentioned above. The additional amounts of DMS or methyl mercaptan can then be separated in the first primary separation unit 20 and then further purified as described above.
The process plant 1 of
The process plant 1 further comprises a flow line 83 for feeding DMS and/or methyl mercaptan from the lignin treatment arrangement 80 to a point in the processing arrangement 2 upstream of the first primary a separation unit 20 where DMS and/or methyl mercaptan is separated from the stream. Additional DMS (or DMSO or methyl mercaptan) can thus be produced, separated and purified in line with what is described above.
The invention is not limited by the embodiments described above but can be modified in various ways within the scope of the claims. Besides the many modifications and variations already described above in relation to the example shown in
| Number | Date | Country | Kind |
|---|---|---|---|
| 2050074-0 | Jan 2020 | SE | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/SE2021/050047 | 1/27/2021 | WO |
