Distillation with vapor recompression

Abstract

The present invention relates to a system for distillation, specifically a system for distillation of a first raw product stream, preferably a raw methanol stream. Specifically, the system comprises a first concentration column arranged to provide a first product stream and a compressor is arranged to receive at least a portion of the first product stream, pressurise said stream, and provide a third product stream with an increased saturation temperature compared to the first product stream. A first reboiler is arranged to receive at least a first portion of the third product stream and provide heat energy to the first concentration column. In this way, the arrangement of the compressor and the first reboiler may result in a lowering of the energy contribution required from outside the system for distillation, which is necessary to drive the purification process of the first raw product stream. The invention further relates to a method for distillation of a first raw product stream and to a chemical plant.

Description

[0001] DISTILLATION WITH VAPOR RECOMPRESSION

[0002] TECHNICAL FIELD

[0003] The present invention relates to a system for distillation, specifically a system for distillation of a first raw product stream, preferably a raw methanol stream. The invention further relates to a method for distillation of a first raw product stream and to a chemical plant.

[0004] BACKGROUND

[0005] Reboilers are heat exchangers typically used to provide heat to industrial distillation columns (typically the bottom thereof). In a typical classical distillation column, most - if not all - the vapor driving the separation comes from the reboiler. The reboiler receives a liquid stream (i.e., a take-off stream) from the column bottom and may partially or completely vaporize it. Following vaporisation, the stream is returned to the column to drive the d istillation process. The heat required for the reboiler is usually provided by steam streams. In traditional chemical plants such low pressure streams may be generated as side product streams during chemical synthesis.

[0006] In recent years, the development of chemical plants and processes strives towards production which enables renewable energy sources to drive production of chemical compounds. One way of achieving this is to use an e-syngas section which through electrolysis of water and / or carbon dioxide can provide an e-syngas, which is suitable for further synthesis of carbon comprising chemical compounds. Within such renewable chemical plants, production of chemical compounds does not necessarily provide a sufficient amount of low pressure steam to supply the necessary energy to drive the distillation process for achieving the high grade purified product stream, such as a high grade purified methanol stream.

[0007] In addition, in relation to existing traditional chemical production plants, an overall reduction of energy consumption of the chemical plant is desirable as such reduction typically also results in an overall lowering of the carbon emissions from said plant.

[0008] In this way, there is a need to reduce the energy consumption in a system for distillation, such as in a distillation system in a chemical plant. Additionally, there may be a need for providing a more flexible heat supply to achieve energy optimization within said system for distillation such as within a chemical plant. SUMMARY

[0009] It has been found by the present inventor(s) that the first product stream provided from a first concentration column holds the potential for introducing additional energy into the production process. To exploit this, a compressor is arranged to receive at least a portion of the first product stream, pressurise said stream, and provide a third product stream with an increased saturation temperature compared to the first product stream. A first reboiler is arranged to receive at least a first portion of the third product stream and provide heat energy to the first concentration column, hereby lowering the energy contribution required from outside the system for distillation, which is necessary to drive the purification process of the first raw product stream.

[0010] So, in a first aspect the present invention relates to a system for distillation, said system comprising : a first raw product stream; a stabilizer section comprising a stabilizer column; a first concentration column; a first heat exchanger, optionally a second heat exchanger; a first compressor; a first reboiler and a second reboiler; a drum; a first pump; wherein the stabilizer section is arranged to receive the first raw product stream and provide a second raw product stream, and a first off-gas stream; wherein the first concentration column is arranged to receive the second raw product stream and distil said stream so as to output a first product steam, a first condensate stream, and optionally a second off-stream; wherein the first heat exchanger is arranged to receive at least a first portion of the first product stream and to output a second product stream; wherein the first compressor is arranged to receive at least a second portion of the first product stream and to output a third product stream; wherein the first reboiler is arranged to receive at least a first portion of the third product stream and provide heat energy to the first concentration column, and wherein at least a portion of the heat energy for the first reboiler is provided from the third product stream such that said first reboiler outputs a fourth product stream; wherein the fourth product stream is arranged to be fed to the inlet of the first heat exchanger together with the first portion of the first product stream, and / or the fourth product stream is arranged to be fed to the inlet of the second heat exchanger so as to output a fifth product stream; wherein the drum is arranged to receive at least a portion of the second product stream and / or at least a portion of the fifth product stream and provide a sixth product stream; wherein the first pump is arranged to receive at least a portion of the sixth product stream from the drum and output a seventh product stream, optionally wherein a portion of said seventh product stream is fed to the first concentration column; wherein the second reboiler is arranged to provide additional heat energy to the first concentration column.

[0011] In a second aspect, the present invention relates to a chemical plant comprising : a first syngas stream; a product synthesis section; the system for distillation according to the system disclosed herein, wherein said product synthesis section is arranged to receive the first syngas stream and output a first raw product stream, and wherein said system for distillation is arranged to receive at least a portion of said first raw product stream from said product synthesis section and output a product stream such as a seventh product stream (71).

[0012] In a third aspect, the present invention relates to an arrangement for district heating, said arrangement comprising : a district heating grid comprising at least one district heating stream, and the chemical plant comprising the system for distillation, wherein the system for distillation further comprises a fifth portion of the third product stream, wherein the district heating grid such as the at least one district heating stream is arranged to receive heat energy from a fifth portion of the third product stream via heat exchange.

[0013] In a fourth aspect, the present invention relates to a method for distillation of a first raw product stream, in the system disclosed herein, wherein said method comprises: feeding a first raw product stream to the stabilizer section and providing a second raw product stream, and a first off-gas stream; feeding at least a portion of the second raw product stream to the first concentration column, distilling said stream and providing a first vaporised product stream from said first concentration column, a first condensate stream, and optionally a second off- stream; feeding at least a first portion of the first product stream to the first heat exchanger, and providing a second product stream from said first heat exchanger; feeding at least a second portion of the first product stream to the first compressor, and providing a third product stream from the first compressor; feeding at least a first portion of the third product stream to the first reboiler, and hereby providing heat to the first concentration column, wherein the step of providing heat to the first concentration column comprises providing heat energy from the at least first portion of the third product stream to the first reboiler and providing a fourth product stream from said first reboiler; feeding at least a portion of the fourth product stream to the inlet of the first heat exchanger together with the first portion of the first product stream, and / or feeding at least a portion of the fourth product stream to the inlet of the second heat exchanger and providing a fifth product stream; feeding at least a portion of the second product stream and / or at least a portion of the fifth product stream to the drum, and providing a sixth product stream, feeding at least a portion of the sixth product stream from drum to the first pump, and providing a seventh product stream, and optionally feeding a portion of said seventh product stream as a fed to the first concentration column; providing addition heat energy to the first concentration column by heat energy transfer from the second reboiler.

[0014] In a fifth aspect, the present invention relates to a method for producing a chemical product stream, in the chemical plant disclosed herein, wherein said method comprises: feeding a first syngas stream to a product synthesis section to output a first raw product stream, feeding at least a portion of said first raw product stream to said system for distillation (200) to output a product stream such as a seventh product stream.

[0015] In a sixth aspect, the present invention relates to a method for district heating, in the arrangement for district heating disclosed herein, wherein said method comprises: indirectly transferring heat energy from the fifth portion of the third product stream to the district heating grid such as to the at least one district heating stream via heat exchange. Further details of the system and process for producing the synthesis gas stream, and the related plants, are specified in the following detailed description, figures, and claims.

[0016] LEGENDS Fig. 1 shows a first schematic drawing of the system for distillation.

[0017] Fig. 2 shows a second schematic drawing of the system for distillation.

[0018] Fig. 3 shows a third schematic drawing of the system for distillation.

[0019] Fig. 4 shows a fourth schematic drawing of the system for distillation.

[0020] Fig. 5 shows a fifth schematic drawing of the system for distillation. Fig. 6 shows a first schematic drawing of a chemical plant and shows a first schematic drawing of an arrangement for district heating.

[0021] Fig. 7 shows a first schematic drawing of the chemical plant.

[0022] DETAILED DISCLOSURE

[0023] Unless otherwise specified, any given percentages for gas content are % by volume. The terms "synthesis gas" and "syngas" are used interchangeably in this text.

[0024] System for distillation

[0025] A system for distillation comprises a first raw product stream; a stabilizer section comprising a stabilizer column; a first concentration column; a first heat exchanger, optionally a second heat exchanger; a first compressor; a first reboiler and a second reboiler; a drum; and a first pump.

[0026] The first raw product stream

[0027] The first raw product stream may be a raw methanol stream, wherein said raw methanol stream comprises methanol (CH3OH). Suitably, the first raw product stream is a liquid stream, hence, preferably, the raw methanol stream comprises liquid methanol, most preferably is a liquid methanol stream. The raw methanol stream may further comprise water (H2O), higher alcohols, such as ethanol and propanol, and light impurities comprising ketones, and dissolved gases, such as CO2. Typically, the raw methanol stream comprises methanol in a concentration of 60-70 % by weight if based on above-mentioned e-syngas. Alternatively, the first raw product stream could also originate from syngases based on reforming of biogas or natural gas or gasification of coal. In this aspect, the first raw product stream is a raw methanol stream, the seventh product stream is a first distilled methanol stream.

[0028] The stabilizer section

[0029] The stabilizer section is arranged to receive the first raw product stream and provide a second raw product stream, and a first off-gas stream.

[0030] The stabilizer section comprises a stabilizer column. The stabilizer section may further comprise an internal first vapor stream, an internal condenser heat exchanger for condensing the internal first vapor stream, an internal drum, and an internal pump. Preferably, the stabilizer column is arranged to provide the internal first vapor stream directly from the top of the column, the internal condenser heat exchanger is arranged to receive at least a portion of the internal first vapor stream and condense said stream to provide an internal condensed stream. The internal drum is arranged to receive at least a portion of the internal condensed stream to provide a first off-gas stream (such as the first off-gas stream provided from the stabilizer section) and a liquid stream, wherein at least a portion of (preferably all of) said liquid stream is arranged to be refluxed to the stabilizer column via the internal pump.

[0031] The stabilizer section removes gases and other light impurities. When the first raw product stream is a raw methanol stream, the first off-gas stream may comprise approx. 80% CO2 and 20% methanol. The stabilizer section is arranged to provide a second raw product stream, which is a purified stream relative to the first raw product stream. Typically, when the first raw product stream is a raw methanol stream, the second raw product stream comprises methanol 60-70 weight%, water 30-40 weight%, ketones less than 500 weight ppm, higher alcohols 500 weight ppm.

[0032] A series of energy-providing arrangements may be implemented to drive the purification process to provide the second raw product stream. Such arrangement may comprise heaters or a transfer of heat energy from a low pressure steam stream to the bottom of the stabilizer column. Such arrangements are described further in this text.

[0033] The first concentration column

[0034] The first concentration column is arranged to receive the second raw product stream and distil said stream so as to output a first product steam, a first condensate stream, and optionally a second off-stream.

[0035] The first concentration column is a column suitable for distillation, preferably a column suitable for methanol distillation. Suitably, the distillation column may comprise trays and / or packings. Generally, a concentration column is understood to comprise a series of equilibrium stages in which two phases establish an equilibrium. The concept of equilibrium stages is well known in the art.

[0036] The first concentration column may be a low pressure distillation column. Typically, the operating pressure of the first concentration column may be between 0.1-10.0 bar g, preferably 0.1-1.5 bar g. Herein operating pressure refers to a pressure measured within any equilibrium stage within said column. The operation temperature interval within the first concentration column may vary dependent on the product desired to be distilled. Suitably, a column for methanol distillation is operated within a temperature interval between 68-125 °C, wherein the temperature interval refers to a temperature measured within any equilibrium stage within said column.

[0037] The first product stream comprises vaporised product, such as 95 % product, or preferably 99 % product. This first product stream may preferably be 99 % methanol. The second off- stream comprises methanol, water and higher alcohols. Typically, the second off-stream is a liquid stream.

[0038] The first condensate stream may be a first distillation water stream, preferably comprising more than 95 weight% water with traces of product, or it may be a stream comprising at least 10 weight% product. Preferably, wherein the system for distillation comprises only the first concentration column, the first condensate stream is a first distillation water stream, wherein the distillation water stream comprises 99 weight% water. Wherein the system for distillation comprises two or more concentration columns, such as a first and a second concentration column, the first condensate stream is a stream comprising at least a portion of the product, such as at between 10-50 weight% product.

[0039] The first reboiler is arranged to provide at least a portion of the necessary energy for driving the distillation within the first concentration column, (i.e. operating within the preferred temperature interval). Generally, a reboiler is arranged to receive a take-off stream and provide a return stream to a column (e.g., stabilizer column or concentration column). Herein, a take-off stream is a liquid take-off stream arranged to be provided from a column and a return stream is a vapor return stream (e.g. comprising vapor) arranged to be returned to the column. In this way, a reboiler may vaporise all the liquid of the take-off stream to provide a vapor return stream or alternatively a reboiler may vaporise a portion of the liquid of the take-off stream to provide a vapor return stream and a liquid return stream.

[0040] The first reboiler may be a side-drawn reboiler such that said first reboiler receives a first take-off stream from the first concentration column and provides a first return stream, arranged to be fed to the first concentration column. In contrast to a reboiler providing heat energy to the bottom of the column, i.e. providing heat energy to the lowest equilibrium stage, the side-drawn reboiler provides heat energy to minimum one equilibrium stage above the lowest equilibrium stage (e.g. at the bottom of the column). At the lowest equilibrium stage, the temperature is higher than all equilibrium stages above, as the temperature decreases going up though the column. The temperature of the first take-off stream is thus lower than the temperature at the bottom of the first concentration column. In this way, a side-drawn reboiler provides heat to a take-off stream. A side-drawn reboiler is also known as an intermediate reboiler.

[0041] Alternatively or additionally, the first reboiler may be arranged to provide heat energy to at least a portion of the second raw product stream from the stabilizer section. This is an alternative way of providing heat energy to the first concentration column. One way of achieving this may be to split the second raw product stream in a first stream comprising at least a portion of the vaporised portion of the second raw product stream and a second stream comprising at least a portion of the liquid portion of the second raw product stream, wherein the first reboiler is arranged to provide heat energy to the second stream, such to vaporise at least a portion of the second stream and provide a third stream, wherein the first stream and the third stream is fed as feeds to the first concentration column as separate streams, or preferably as a combined stream. Another way of achieving this is to provide heat energy to the second raw product stream from the stabilizer section to provide a first stream comprising a vapor stream, and optionally a second stream comprising a liquid stream, and feed the first stream and optionally also the second stream to the first concentration column.

[0042] The second reboiler is arranged to provide additional heat energy to the first concentration column. The second reboiler may be arranged to provide heat energy to the bottom of the first concentration column, wherein said second reboiler receives a second take-off stream from the first concentration column and provides a second return stream, arranged to be fed to the first concentration column. The arrangement comprising the second take-off stream and the second return stream is specifically suitable, when the first reboiler is arranged to be a side-drawn reboiler or when the first reboiler is arranged to provide heat energy to the second raw product stream.

[0043] The first reboiler and the second reboiler may alternatively be arranged to provide heat energy to the bottom of the first concentration column, preferably wherein at least one of the first and / or second reboiler receives at least a portion of a third take-off stream and wherein the first and / or second reboiler is arranged to provide at least one third return stream to the first concentration column. The first reboiler and the second reboiler may thus be arranged to be within the same circuit of streams, meaning that both the first and the second reboiler may be connected to the third take-off stream and the third return stream.

[0044] The specific arrangement of the third take-off stream, the return stream and the first and second reboiler can be varied. In a preferred arrangement, the first reboiler is arranged to receive the third take-off stream and provide a first stream and a second stream, wherein the first stream comprises vaporised product and the second stream comprises liquid product. The second reboiler is arranged to receive the second stream and provide a third stream comprising vaporised product. The first concentration column is then arranged to receive the first stream and / or the third stream as at least one return stream, preferably the first and the third stream is combined and fed to the first concentration column as the third return stream. In a second alternative preferred arrangement, the third take-off stream is split in a first stream comprising a first portion of the third take-off stream and a second stream comprising a second portion of the third take-off stream. The first reboiler is arranged to receive the first stream and outputs a third stream comprising vaporised product and the second reboiler is arranged to receive the second stream and outputs a fourth stream comprising vaporised product. The first concentration column is then arranged to receive the third stream and / or the fourth stream as at least one return stream, preferably the third and the fourth stream is combined and fed to the first concentration column as the third return stream. An equally suitable arrangement is achieved, if the first reboiler and the second reboiler are interchanged within the second preferred arrangement.

[0045] In this way, independent of the specific arrangement of the first reboiler and the second reboiler, both the first reboiler and second reboiler contribute to driving the distillation process within the first concentration column.

[0046] Product streams and vapor recompression

[0047] The first product stream comprises vaporised product. A portion of the first product stream may be condensed and exported as a high-grade purified product stream. Optionally, this high-grade purified product stream may be arranged to be combined with other high grade purified product streams provided within the system for distillation (specifically with a portion of the seventh product stream and / or a portion of the eleventh product stream, to be described below). However, the first product stream also holds the potential for introducing additional energy into the production process. To exploit this, the first heat exchanger is arranged to receive at least a first portion of the first product stream and to output a second product stream, and the first compressor is arranged to receive at least a second portion of the first product stream and to output a third product stream. In this way, the compressor is arranged to receive the vaporised first product stream, pressurise said stream, and provide a third product stream with an increased saturation temperature compared to the first product stream. Preferably, the third product stream is a compressed and superheated vapor.

[0048] The first compressor may further be arranged to receive a pure product stream, wherein the pure product stream is arranged to provide injection cooling. Advantageously, injection cooling is a way of cooling gas (e.g. the second portion of the first product stream) before a next compression stage. More specifically, injection cooling allows for i) lowering power consumption of the next compression stage due to smaller volume flow and further ii) limiting the risk of exceeding potential temperature limits for certain materials comprised within the compressor. In this way, injection cooling allows for the third product stream to be further compressed than suitable without injection cooling.

[0049] A pure product stream is used to refer to a product stream, which essentially comprises product such as at least 60wt% product, however preferably above 90wt% product such as above 95wt% product, more preferably above 98wt% product, most preferably 99wt% product or above 99wt% product. Most preferably, the pure product stream has a purity equal to or above the sixth product stream, wherein purity is to be understood as wt% product such as wt% methanol of said stream. The pure product stream may be fuel grade methanol or AA grade methanol or equivalent standards. The pure product stream arranged to be received by the first compressor may comprise i) a portion of the sixth product stream provided from the drum, optionally provided to the first compressor via a pump, ii) a second portion of said seventh product stream, iii) a pure product stream from storage such as from a product storage tank or any combination thereof. Specifically, the product storage tank may be a methanol storage tank.

[0050] Preferably, at least a second portion of the seventh product stream is fed as a feed to the first compressor. The advantage of a pure product stream such as a second portion of the seventh product stream being fed as a feed to the first compressor is that the pure product acts as a cooling liquid such regulates (e.g. reduces) the temperature of the stream within the first compressor (e.g. provide injection for cooling so the temperature is reduced) such to provide a third product stream.

[0051] The first compressor may comprise one or more compression stages. The pure product stream arranged to be received by the first compressor may be arranged to be split into substreams, wherein such sub-streams may be arranged to be fed as feed(s) upstream or downstream compression stage(s). The term upstream is here used to refer to just prior to a compression stage whereas the term downstream is used to refer to just after a compression stage. This allows for a sub-portion of the pure product stream to be arranged to be fed as feed(s) just prior to any compression stage or just after any compression stage within the first compressor hereby providing injection cooling. Typically, the number of sub-streams within said compressor is equal to the number of compression stages comprised within the first compressor or the number of sub-streams within said first compressor is ±1 of the number of compression stages comprised within the first compressor. In this way, the pure product stream such as one or more sub-streams thereof may be arranged to be provided to the first compressor between any two compression stages, optionally also before the initial compression stage and / or after the final compression stage. Consequently, there may be injection cooling between any two stages and possibly also before the first and after the last compression stage.

[0052] Specifically, wherein the first compressor comprises one compression stage, at least one substream of the pure product stream such as of the second portion of the seventh product stream may be arranged to be fed as a feed upstream and / or downstream of the compression stage.

[0053] Specifically, wherein the first compressor comprises two or more compression stages, one or more sub-stream(s) of the pure product stream such as of the second portion of the seventh product stream may be arranged to be provided to the first compressor between any two compression stages, optionally also before the initial compression stage and after the final compression stage.

[0054] Independent on the specific arrangement of sub-steams within said first compressor, each of the sub-streams may be turned on, off or be throttled individually as required. Herein turned on is used to refer to the sub-stream being partly or fully open such as l%-100% open, off is used to refer to the sub-stream being fully closed such being 0% open and throttled is used to refer to the sub-stream being less than fully open such as 1-99% open. This is advantageous because the operation of each compression stage can be precisely controlled and the full potential of the first compressor can be exploited.

[0055] The first reboiler is arranged to receive at least a first portion of the third product stream and provide heat energy to the first concentration column. At least a portion of the heat energy for the first reboiler is provided from the third product stream such that said first reboiler outputs a fourth product stream. Preferably, the first reboiler allows for the condensation heat of the first portion of the third product stream to be released as heat energy and further for the transfer of said heat energy to the first concentration column. Therefore, the first reboiler may condense at least the first portion of the third product stream into a liquid so as to output the fourth product stream being the condensed liquid, optionally further comprising vapor not condensed in the first reboiler. In this way, the arrangement of the compressor and the first reboiler may result in a lowering of the energy contribution required from outside the system for distillation, which is necessary to drive the purification process of the first raw product stream.

[0056] The fact that the first compressor is arranged to receive at least a second portion of the first product stream and not limited to receiving all the first product stream, provides the advantage that it allows for the increase or decrease of the heat energy transferred to the first concentration column via the compressor and reboiler. If all of the first product stream is sent to the compressor, the system is less flexible and may rely on other reboiler(s) operating on another heat source, wherein other heat source such as steam may be limited. In this way, arranging the system such that the compressor receives a portion of the first product stream may provide a more flexible heat supply within the system for distillation.

[0057] In embodiments, the first reboiler may be a side-drawn reboiler such that said first reboiler receives a first take-off stream from the first concentration column and provides a first return stream, arranged to be fed to the first concentration column. The first reboiler may transfer heat from the first portion of the third product stream to the first take-off stream via heat exchange so as to provide the (heated) first return stream. This is one way in which the first reboiler may be arranged to provide heat energy to the first concentration column, wherein at least a portion of the heat energy for the first reboiler is provided from the first portion of the third product stream.

[0058] The temperature of the first take-off stream from the first concentration column is lower than the temperature by the second reboiler, wherein the second reboiler is arranged to provide heat energy to the bottom of the first concentration column. Arranging the first reboiler to be a side-drawn reboiler has the advantage that the saturation temperature of the first portion of the third product stream received by the first reboiler does not need to be as high compared to if the first reboiler is arranged to driving a bottom reboiler. Hence, the required pressure outlet at the compressor can be reduced compared to driving a bottom reboiler. Thus, arranging the first reboiler to be a side-drawn reboiler may reduce not only the power consumption but also the number of compression stages required for compression (i.e., reduction of compressor equipment).

[0059] In embodiments, the first reboiler may be arranged to provide heat energy to the second raw product stream from the stabilizer section. This means that the first reboiler may transfer heat from the first portion of the third product stream to the second raw product stream. This is an alternative way the first reboiler may be arranged to provide heat energy to the first concentration column, wherein at least a portion of the heat energy for the first reboiler is provided from the first portion of the third product stream.

[0060] The first reboiler and the second reboiler may be arranged to provide heat energy to the bottom of the first concentration column, preferably wherein at least one of the first and / or second reboiler receives at least a portion of a third take-off stream and such that the first reboiler is arranged to receive heat from the first portion of the third product stream and wherein the first and / or second reboiler is arranged to provide at least one third return stream to the first concentration column. Hence, the first reboiler is arranged to provide at least a portion of the heat energy comprised in the third return stream which is fed to the first concentration column.

[0061] Independently of the specific arrangement of the first reboiler, the first reboiler is arranged to operate at a saturation temperature of the first portion of the third product stream between 75 °C and 140 °C. This interval is suitable for vaporising the first or third take-off stream and further optimises the energy balance between the energy needed to drive the first compressor and the heat energy available in the (heated) first portion of the third product stream provided by the first compressor.

[0062] Again, independently of the specific arrangement of the first reboiler (i.e. independently of where-to the third product stream heat is transferred), the first reboiler outputs a fourth product stream, which comprises less heat than (i.e. condensed compared to) the first portion of the third product stream. The fourth product stream is arranged to be fed to the inlet of the first heat exchanger together with the first portion of the first product stream, and / or the fourth product stream is arranged to be fed to the inlet of the second heat exchanger so as to output a fifth product stream. The drum is arranged to receive at least a portion of the second product stream and / or at least a portion of the fifth product stream and provide a sixth product stream. In this way, the one or more heat exchangers are arranged to fully condense, optionally sub-cool, the product stream(s) (first portion of the first product stream, and / or the fourth product stream and / or the fifth product stream) at the drum's operating pressure and the drum is arranged to receive one or more condensed product streams. The drum is further arranged to provide the sixth product stream, which is preferably a liquid product stream. The first pump is arranged to receive at least a portion of the sixth product stream from the drum and output a seventh product stream, optionally wherein a portion of said seventh product stream is fed to the first concentration column. The first portion of said seventh product stream is preferably a condensed product stream, which is refluxed to the first concentration column. Hence, the first portion of said seventh product stream refluxed to the first concentration column is in liquid phase. The reflux of a portion of said seventh product stream to the first concentration column results in an increased purity of the seventh product stream such to reach sufficient purity grades of the produced product.

[0063] Vapor recompression for driving the stabilizer column

[0064] To optimise the energy consumption and distribution of heat energy generated within said system for distillation, it may be valuable to also provide a second portion of the third product stream. The heat energy of this second portion of the third product stream may be used to drive the purification process within the stabilizer column.

[0065] Specifically, the stabilizer column may be arranged to receive heat energy from a second portion of the third product stream, preferably said system further comprises a third reboiler, wherein said third reboiler is arranged to receive a fourth take-off stream and provide a fourth return stream, and wherein at least a portion of the heat energy of the second portion of the third product stream is arranged to be transferred to the fourth take-off stream. This arrangement may significantly lower the energy needed to be provided from external energy sources (i.e. from outside the system for distillation) to drive the purification process within said stabilisation column.

[0066] The third reboiler may be arranged to output a condensed second portion of the third product stream. At least a portion of the condensed second portion of the third product stream may be arranged to be fed to the inlet of one of i) the first heat exchanger, ii) the optional second heat exchanger, or optionally a third heat exchanger, wherein the third heat exchanger is arranged to provide an additional product feed arranged to be fed to the drum.

[0067] Energy for the second reboiler series of energy-providing arrangements may be implemented in order for the second reboiler to be arranged to provide additional heat energy to the first concentration column. Such energy-providing arrangements may be electric heaters, or a transfer of heat energy from a product stream (i.e. comprising excess heat otherwise wasted) or from a low pressure steam stream or steam condensate stream, both of which may be available within said system for distillation or within said chemical plant. Herein, a low pressure steam stream or a steam condensate stream preferably has a saturation pressure between 3.5-10.0 bar g. Specifically preferred, the second reboiler may be arranged to transfer heat energy from at least a portion of an eighth product stream provided from a second concentration column comprised within said system for distillation.

[0068] Specifically, the system may further comprise a second concentration column, a second drum, a second pump, and a fourth reboiler and wherein said second concentration column is arranged to receive at least a portion of the first condensate stream and provide an eighth product stream, a second condensate stream, and a third off-stream, and wherein said fourth reboiler is arranged to provide heat energy to the second concentration column, wherein the second reboiler is arranged to receive at least a portion of the eighth product stream to output a ninth product stream, wherein said second drum is arranged to receive at least a portion of said ninth product stream and output a tenth product stream, and wherein said second pump is arranged to receive at least a portion of the tenth product stream and provide an eleventh product stream, wherein a first portion of said eleventh product stream is arranged to be fed as a feed to the second concentration column, and optionally, wherein a second portion of said eleventh product stream is arranged to be combined with at least a portion of said seventh product stream.

[0069] The system for distillation may comprise additional concentration columns, such as two or more condensation columns. The second concentration column may be a medium pressure distillation column. Typically, the operating pressure of the second concentration column (90) is between 2.5-10.0 bar g such as preferably between 2.5-7.0 bar g, such as preferably 3.5- 5.5 bar g. Typically, the operating pressure of the second concentration column is above the operating pressure of the first concentration column. The eighth product stream comprises vaporised product, such as 97 vol% product, or preferably 99 vol% product. This eighth product stream may preferably be 99 vol% methanol. The third off-stream may comprise methanol, water and higher alcohols. Typically, the third off-stream is a liquid stream.

[0070] The second condensate stream may be a second distillation water stream, or it may be a stream comprising at least a portion of the product. Preferably, wherein the system for distillation comprises only the first and the second concentration column, the second condensate stream is a first distillation water stream, wherein the distillation water stream comprises 99 weight% water.

[0071] The fourth reboiler is arranged to provide at least a portion of the necessary energy for driving the distillation within the second concentration column, (i.e operating within the preferred temperature interval). Specifically, the fourth reboiler is arranged to provide heat energy to the bottom of the second concentration column, preferably wherein the fourth reboiler is arranged to receive a fifth take-off stream and provide a fifth return stream, wherein at least a portion of the fifth return stream is arranged to be fed to the second concentration column.

[0072] Heat integration

[0073] Implementing additional heat integration designs within the system for distillation results in a further reduction of the energy consumption of the distillation system and / or the chemical plant (e.g. by removing otherwise necessary external heating arrangements). Herein, heat integration designs refer to system designs which allow streams with excess heat energy that would otherwise be wasted in air cooler or water cooler to be arranged to provide heat energy to one or more stream(s). This means that the system for distillation can be designed such that steams comprising excess heat energy may transfer said excess heat via heat exchange to one or more streams such as to one or more product streams or take-off streams within the system for distillation.

[0074] The first reboiler, which is arranged to provide heat energy to the first concentration column, the first reboiler is arranged to receive at least the first portion of the third product stream and output the fourth product stream. The fourth product stream preferably comprises a condensed product stream. Likewise, the third reboiler may be arranged to provide heat energy to the stabilizer concentration column, the third reboiler may be arranged to receive at least a second portion of the third product stream and output a condensed second portion of the third product stream, preferably comprising a condensed product stream. The fourth product stream and the condensed second portion of the third product stream may still comprise available heat energy compared to the first raw product stream, the second raw product stream and / or the first condensate stream. Thus, the excess heat energy of the fourth product stream and the condensed second portion of the third product stream may be arranged to be transferred to the first raw product stream, the second raw product stream and / or the first condensate stream via heat exchange (such as via the first or second heat exchanger). This may be even further generalized as any condensed product stream from any reboiler within the system for distillation (e.g. also the ninth product stream from the second reboiler) may comprise available excess heat energy for preheating other streams, preferably first raw product stream, the second raw product stream and / or the first condensate stream via heat exchange. Depending on the type of heat exchanger the temperature difference between stream within such heat exchanger may be between 3 °C - 100 °C.

[0075] The second reboiler, which is arranged to provide additional heat energy to the first concentration column, may receive heat energy from a low pressure steam stream. Within this embodiment, the second reboiler may be arranged to receive a first low pressure steam stream and output a first steam condensate stream, wherein excess heat energy of the first steam condensate stream is arranged to be transferred by heat exchange to at least one of i) the first raw product stream, ii) the second raw product stream from the stabilizer section, and iii) the stabilizer column as reboiling heat, preferably to the stabilizer column as reboiling heat. Transferring the excess heat energy of the first steam condensate stream to the stabilizer column as reboiling heat is preferred, because it allows for phase transition of the stream being heated.

[0076] The first concentration column is arranged to output a first condensate stream. In embodiments, at least a portion of the excess heat energy of the first condensate stream from the first concentration column may be arranged to be transferred by heat exchange to at least one of i) the first raw product stream, ii) the second raw product stream from the stabilizer section, and iii) the stabilizer column as reboiling heat, preferably to the i) the first raw product stream and / or ii) the second raw product stream. Transferring excess heat energy from the first condensate stream to the first and / or second raw product stream may be favourable, because the amount of excess heat energy in the first condensate stream is suitable for heating a process stream without inducing undesired phase transition processes within said process stream. The transfer of excess heat energy to more than one stream, may be achieved by arranging a first transfer of excess heat energy to one stream followed by transfer of a remaining excess heat energy to a second stream. Specifically, the first condensate stream may be arranged to transfer heat energy to the second raw product stream followed by a further transfer of heat energy to the first raw product stream. Excess heat energy may also be available from internal streams within the stabilizer section or from streams used to drive purification within the stabilizer column. In embodiments, wherein the stabilizer section further comprises an internal first vapor stream, an internal condenser heat exchanger, an internal drum, and an internal pump, and wherein the stabilizer column is arranged to provide the internal first vapor stream directly from the top of the column, the excess heat energy of the internal first vapor stream is arranged to be transferred to the first raw product stream by heat exchange.

[0077] Additionally or alternatively, in embodiments comprising the third reboiler, which is arranged to provide heat energy to the stabilizer column, the third reboiler is arranged to receive the second portion of the third product stream and output a condensed second portion of the third product stream. The condensed second portion of the third product stream may still comprise available heat energy compared to the first raw product stream. Thus, the excess heat energy of the condensed second portion of the third product stream may be arranged to be transferred to the first raw product stream via heat exchange followed by said stream being fed to the drum.

[0078] In embodiments comprising the second concentration column, excess heat energy may also be available from streams used to drive purification within the second concentration column or from streams provided by the second concentration column. Thus, in embodiments comprising the second concentration column providing a second condensate stream, at least a portion of the excess heat energy of the second condensate stream may be arranged to be transferred by heat exchange to at least one of i) the first raw product stream, ii) the second raw product stream from the stabilizer section, iii) the first condensate stream from the first concentration column and iv) the stabilizer column as reboiling heat, preferably to the first condensate stream and / or the first raw product stream. Again, the transfer of excess heat energy to more than one stream, may be achieved by arranging a first transfer of excess heat energy to one stream followed by transfer of a remaining excess heat energy to a second stream. Thus, the second condensate stream may be arranged to transfer heat energy to the first condensate stream followed by a further transfer of heat energy to the first raw product stream.

[0079] Alternatively or additionally, in embodiments comprising the second concentration column and the fourth reboiler, the fourth reboiler may be arranged to receive a second low pressure steam stream and output a second steam condensate stream, and optionally, wherein excess heat energy of the second steam condensate stream is arranged to be transferred by heat exchange to at least one of i) the first raw product stream, ii) the second raw product stream from the stabilizer section, iii) the first condensate stream from the first concentration column and iv) the stabilizer column as reboiling heat, preferably to the stabilizer column. The different embodiments disclosing heat integration designs may be combined in multiple ways. In this way, the system may comprise arrangement such that heat energy is arranged to be transferred from one or more streams within the system for distillation to one or more streams within the system for distillation. This may be achieved by transfer of excess heat to one stream followed by transfer of a remaining excess heat energy to a second stream (i.e. transferring heat energy from one stream) and / or arranging heat transfer from more than one stream to at least one stream. Interestingly, combining vapor recompression for driving the stabilizer column with heat integration, wherein excess heat energy is arranged to be transferred to more than one stream may provide the required energy efficiency to drive the purification process within said stabilisation column such that no additional energy needs to be provided to the stabilizer column. Even more interestingly, combining vapor recompression for driving the first concentration column with heat integration, wherein excess heat energy is arranged to be transferred to more than one stream may provide required energy efficiency within the system for distillation such that low pressured steam streams generated by excess heat in an e-syngas and / or synthesis section within a chemical plant can provide sufficient heat energy to the system for distillation and hereby balancing the energy consumption. This means that no additional heaters are required within the chemical plant.

[0080] As an example, in a system for distillation further comprising the second concentration column with the second condensate stream and the fourth reboiler arranged to output the second steam condensate stream, and wherein the stabilizer section further comprises an internal first vapor stream, an internal condenser heat exchanger, an internal drum, and an internal pump, wherein said stabilizer column is arranged to provide the internal first vapor stream directly from the top of the column, it may be preferred to combine i) heat integration designs where at least a portion of the excess heat energy of the second condensate stream is arranged to be transferred by heat exchange to the first condensate stream, followed by additional heat energy transfer to the first raw product stream, with ii) heat integrations designs where excess heat energy of the second steam condensate stream is arranged to be transferred by heat exchange to the stabilizer column as reboiling heat and further with iii) heat integration designs where excess heat energy of the internal first vapor stream may be arranged to be transferred to the first raw product stream by heat exchange.

[0081] Chemical plant chemical plant is also provided, said chemical plant comprising : a first syngas stream; a product synthesis section; the system for distillation according to the system disclosed herein, wherein said product synthesis section is arranged to receive the first syngas stream and output a first raw product stream, and wherein said system for distillation is arranged to receive at least a portion of said first raw product stream from said product synthesis section and output a product stream such as a seventh product stream.

[0082] Typically, the syngas stream comprises hydrogen, carbon monoxide and carbon dioxide. The composition of a syngas stream may vary depending on the plant, however suitable compositions are known in the art. The syngas stream may be provided from any suitable source(s).

[0083] The chemical plant may further comprise a carbon source feed such as a natural gas feed or a gasification coal feed and further comprise a reformer section. The reformer section may be any type of reformer section known from the art suitable for such plant. The reformer section may be arranged to receive the carbon source feed and output a syngas stream. Preferably, the reformer section is arranged to provide at least a portion of the first syngas stream. Alternatively, the reformer section may be arranged to provide a first hydrogen stream, a first carbon monoxide stream and / or a first carbon dioxide stream, wherein the first hydrogen stream, the first carbon monoxide stream and / or the first carbon dioxide stream may be arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide / carbon dioxide to provide the first syngas stream. Consequently, the syngas stream may comprise hydrogen, carbon monoxide and carbon dioxide provided from natural gas, such as provided from steam reforming of natural gas or from gasification of coal.

[0084] The chemical plant may further comprise a first H2O feed and an e-syngas section comprising at least one solid oxide electrolysis cell (SOEC) for electrolysis of H2O. The first H2O feed may be a steam feed. The e-syngas section may be arranged to receive the first H2O feed and output a second hydrogen stream. Preferably, at least a portion of said second hydrogen stream may be arranged to be admixed with one or more stream(s) comprising carbon monoxide / carbon dioxide to provide the first syngas stream. Consequently, the first syngas stream may comprise hydrogen provided from electrolysis of H2O.

[0085] The first H2O feed being a steam feed may be provided from an evaporator. This evaporator may herein be referred to as an electrolysis evaporator. Specifically, the electrolysis evaporator may be arranged to receive a water feed and to output the first H2O feed. The electrolysis evaporator may be arranged to comprise boiling water. The heat energy to drive production of the first H2O feed being a steam feed provided by said electrolysis evaporator may be provided from any source such as electric heating or from the system for distillation. The chemical plant may further comprise a first carbon dioxide feed and an e-syngas section comprising at least one SOEC for electrolysis of carbon dioxide. The e-syngas section may be arranged to receive the first carbon dioxide feed and output a second carbon monoxide stream. Preferably, at least a portion of said second carbon monoxide stream is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon dioxide to provide the first syngas stream. Consequently, the first syngas stream may comprise carbon monoxide provided from electrolysis of CO2.

[0086] Hence, the e-syngas section may comprise at least one SOEC for electrolysis of H2O, wherein said e-syngas section is arranged to receive a first H2O feed and provide a second hydrogen stream. Additionally, the e-syngas section may further comprise a SOEC for electrolysis of carbon dioxide, said e-syngas section being arranged to receive a first carbon dioxide feed and provide a second carbon monoxide stream. Additionally, or alternatively, the e-syngas section may comprise at least one SOEC for electrolysis of H2O and CO2, wherein said at least one SOEC is arranged to receive the first H2O feed and the first carbon dioxide feed and output a syngas stream.

[0087] The chemical plant may further comprise a second carbon dioxide feed and a carbon capture unit such as an amine wash. The carbon capture unit is arranged to receive the second carbon dioxide feed and output a second carbon dioxide stream. Hence, the carbon capture unit is arranged to provide a carbon dioxide stream of high purity such as a purity of above 99 vol% carbon dioxide. Preferably, at least a portion of said second carbon dioxide stream may be arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream. Consequently, the first syngas stream may comprise carbon dioxide provided from a carbon capture unit.

[0088] Hence, the chemical plant may comprise the e-syngas section comprising at least one SOEC for electrolysis of H2O and a carbon capture unit such as an amine wash, wherein said e- syngas section is arranged to receive a first H2O feed and provide a second hydrogen stream, and wherein the carbon capture unit is arranged to receive a second carbon dioxide feed and output a second carbon dioxide stream, and wherein at least a portion of said second hydrogen stream is arranged to be admixed with at least a portion of said second carbon dioxide feed to provide the first syngas stream.

[0089] Also a specified chemical plant is provided, said chemical plant comprising : a H2O rich-feed; a CC -rich feed; an e-syngas section; a product synthesis section; and the system for distillation according to the disclosure herein, wherein said e-syngas section is arranged to receive said H2O rich-feed and said CC -rich feed, and output a syngas stream, said product synthesis section is arranged to receive at least a portion of said syngas stream and output a first raw product stream, and wherein said system for distillation is arranged to receive said first raw product stream from said product synthesis section, wherein the e-syngas section and / or the product synthesis section is / are arranged to provide additional heat energy to at least one of i) the first raw product stream, ii) the stabilizer column, iii) the first condensate stream from the first concentration column, optionally iv) the second concentration column and optionally the fourth reboiler, such as through heat exchange. Preferably, said e-syngas section is an SOEC, an alkaline electrolyser or a proton exchange membrane (PEM) arranged to provide a steam stream, wherein said steam stem may be arranged to provide additional heat energy to at least one of i) the first raw product stream, ii) the stabilizer column, iii) the first condensate stream from the first concentration column, optionally iv) the second concentration column and optionally the fourth reboiler through heat exchange. Preferably, the product synthesis section is arranged to provide a steam stream, wherein said steam stem may be arranged to provide additional heat energy to at least one of i) the first raw product stream, ii) the stabilizer column, iii) the first condensate stream from the first concentration column, optionally iv) the second concentration column and optionally the fourth reboiler through heat exchange.

[0090] Specifically, the chemical plant may be a methanol plant, said methanol plant comprising a methanol synthesis section, said methanol synthesis section being arranged to receive a syngas stream and output the seventh product stream.

[0091] The chemical plant arranged to receive additional heat energy from the system for distillation

[0092] Specifically suitable for a chemical plant comprising an e-syngas section comprising at least one SOEC such as at least one SOEC for electrolysis of H2O, at least one SOEC for electrolysis of carbon dioxide (CO2) and / or at least one SOEC for electrolysis of H2O and CO2, the e- syngas section may be arranged to receive heat energy from the system for distillation. Within the system for distillation, the first compressor is arranged to output a third product stream. Said system may further comprise a third portion of the third product stream, wherein said third portion of the third product stream may comprise heat energy. The chemical plant may such comprise an e-syngas section comprising at least one SOEC and the system for distillation further comprising a third portion of the third product stream, wherein the e-syngas section and / or any of the feeds received by the e-syngas section (i.e. first H2O feed and / or first carbon dioxide feed) is arranged to receive heat energy from a third portion of the third product stream via heat exchange.

[0093] Specifically, the chemical plant may comprise an e-syngas section comprising at least one SOEC for electrolysis of H2O and the system for distillation may further comprise a third portion of the third product stream, wherein the e-syngas is arranged to receive the first H2O feed and output a second hydrogen stream, wherein the first H2O feed is arranged to receive heat energy from a third portion of the third product stream via heat exchange. In this way, the chemical plant allows for indirectly transfer of heat energy from the third portion of the third product stream to the first H2O feed via heat exchange.

[0094] Preferably, the chemical plant may comprise an e-syngas section comprising at least one SOEC for electrolysis of H2O, said e-syngas may further comprise the electrolysis evaporator arranged to receive a water feed and to output the first H2O feed. The electrolysis evaporator may be arranged to comprise boiling water. Said electrolysis evaporator may be arranged to receive heat energy from the system for distillation. Within the system for distillation, the first compressor is arranged to output a third product stream. Said system may further comprise a third portion of the third product stream, wherein said third portion of the third product stream may comprise heat energy. Hence, the chemical plant may comprise an e- syngas section, an electrolysis evaporator, and the system for distillation further comprising a third portion of the third product stream, wherein the e-syngas section is arranged to receive a first H2O feed, and wherein the electrolysis evaporator is arranged to receive a water feed, comprise boiling water, and output the first H2O feed, wherein the boiling water comprised in the electrolysis evaporator, the water feed and / or the first H2O feed is arranged to receive heat energy from the third portion of the third product stream. Specifically, the electrolysis evaporator may be arranged to receive the water feed and output the first H2O feed, and further be arranged to receive at least a portion of the third portion of the third product stream and output a condensed third portion of the third product stream, such to transfer heat energy from at least a portion of the third portion of the third product stream to the water feed and / or to the boiling water comprised in the electrolysis evaporator. In this way, the electrolysis evaporator allows for indirectly transferring heat energy from the third portion of the third product stream to the water feed and / or to the boiling water comprised in the electrolysis evaporator so as to evaporate water and output the first H2O feed.

[0095] Suitably, said system for distillation may further comprise a second compressor arranged to receive at least a portion of said third portion of the third product stream such that the e- syngas section and / or any of the feeds received by the e-syngas section is arranged to receive the third portion of the third product stream via a second compressor. In this way, the second compressor is arranged to add additional heat energy to the third portion of the third product stream, suitably to provide additional heat energy to the at least one SOEC. Preferably, the heat energy needed for driving the SOEC may all be provided from the system for distillation.

[0096] Specifically suitable for a chemical plant comprising a carbon capture unit such as an amine wash, the carbon capture unit may be arranged to receive heat energy to drive the carbon capture unit. Preferably, said carbon capture unit may be arranged to receive heat energy from the system for distillation. Within the system for distillation, the first compressor is arranged to output a third product stream. Said system may further comprise a fourth portion of the third product stream, wherein said fourth portion of the third product stream may comprise heat energy. Hence, the chemical plant may comprise a carbon capture unit arranged to receive a second carbon dioxide feed and the system for distillation further comprising a fourth portion of the third product stream, and the carbon capture unit and / or the second carbon dioxide feed may be arranged to receive heat energy from a fourth portion of the third product stream via heat exchange.

[0097] Specifically, the carbon capture unit may comprise a stripper reboiler arranged to comprise a CC -rich liquid. The term "CC -rich liquid" may be used to refer to any liquid suitable for use in an an amine wash comprising CO2. During production of the second carbon dioxides stream, the CC -rich liquid is heated in the stripper reboiler thereby releasing CO2 gas to provide the second carbon dioxides stream. Hence, the chemical plant may comprise a carbon capture unit arranged to receive a second carbon dioxide feed and the system for distillation further comprising a fourth portion of the third product stream, wherein the carbon capture unit further comprises a stripper reboiler and the stripper reboiler further comprises a CC -rich liquid, and wherein the CCh-rich liquid comprised in the stripper reboiler and / or the second carbon dioxide feed is arranged to receive heat energy from a fourth portion of the third product stream via heat exchange. Hence, the stripper reboiler allows for indirect transfer of heat energy from the fourth portion of the third product stream to the CCh-rich liquid comprised in the stripper reboiler via heat exchange so as to output the second carbon dioxide steam. Indirect transfer of heat energy is used to refer to transfer wherein streams do not intermix.

[0098] An arrangement for district heating

[0099] An arrangement for district heating may additionally be provided comprising the chemical plant as described herein and a district heating grid comprising at least one district heating stream. The district heating grid may further comprise a district heating system and / or one or more district heating units for receiving heat energy. District heating units may be domestic heating units. Specifically, the district heating grid may receive heat energy from the system for distillation. Within the system for distillation, the first compressor is arranged to output a third product stream. Said system for distillation may further comprise a fifth portion of the third product stream, wherein said fifth portion of the third product stream may comprise heat energy. The arrangement for district heating may such comprise a district heating grid comprising at least one district heating stream and the chemical plant comprising the system for distillation, wherein the system for distillation further comprises a fifth portion of the third product stream, wherein the district heating grid such as the at least one district heating stream is arranged to receive heat energy from a fifth portion of the third product stream via heat exchange. In this way, the system for distillation may provide additional heat energy for domestic heating.

[0100] A method for distillation of a first raw product stream

[0101] A method for distillation of a first raw product stream is provided in the system as described herein, wherein said method comprises: feeding a first raw product stream to the stabilizer section and providing a second raw product stream, and a first off-gas stream; feeding at least a portion of the second raw product stream to the first concentration column, distilling said stream and providing a first vaporised product steam from said first concentration column, a first condensate stream, and optionally a second off- stream; feeding at least a first portion of the first product stream to the first heat exchanger, and providing a second product stream from said first heat exchanger; feeding at least a second portion of the first product stream to the first compressor, and providing a third product stream from the first compressor; feeding at least a first portion of the third product stream to the first reboiler, and hereby providing heat to the first concentration column, wherein the step of providing heat to the first concentration column comprises providing heat energy from the at least first portion of the third product stream to the first reboiler and providing a fourth product stream from said first reboiler; feeding at least a portion of the fourth product stream to the inlet of the first heat exchanger together with the first portion of the first product stream, and / or feeding at least a portion of the fourth product stream to the inlet of the second heat exchanger and providing a fifth product stream; feeding at least a portion of the second product stream and / or at least a portion of the fifth product stream to the drum, and providing a sixth product stream, feeding at least a portion of the sixth product stream from drum to the first pump, and providing a seventh product stream, and optionally feeding a portion of said seventh product stream as a fed to the first concentration column; providing addition heat energy to the first concentration column by heat energy transfer from the second reboiler.

[0102] Preferably, the method may further comprise that the operating pressure of the first concentration column may be between 0.1-10.0 bar g, preferably 0.1-1.5 bar g. The operating pressure interval here provided relates to the preferred pressure within the column (i.e., independently of whether measured at the top or at the bottom).

[0103] The method may further comprise the step of transferring at least a portion of the excess heat energy of the first condensate stream to at least one of i) the first raw product stream, ii) the second raw product stream from the stabilizer section, and iii) the stabilizer column as reboiling heat.

[0104] In one aspect of the method, wherein said system further comprises a second concentration column, a second drum, a second pump, and a fourth reboiler, said method further comprises: feeding at least a portion of the first condensate stream from the first concentration column to the second concentration column and providing an eighth product stream and a third off-stream; providing heat energy to the second concentration column by heat energy transfer from the fourth reboiler; feeding at least a portion of the eighth product stream to the second reboiler and providing a ninth product stream; feeding at least a portion of said ninth product stream to the second drum and providing a tenth product stream; feeding at least a portion of the tenth product stream to the second pump and providing an eleventh product stream; feeding a first portion of said eleventh product stream as a feed to the second concentration column, and optionally, combining a second portion of said eleventh product stream with at least a portion of said seventh product stream.

[0105] In embodiments comprising the second concentration column, the method may further comprise that the operating pressure of the second concentration column is between 2.5- 10.0 bar g such as preferably between 2.5-7.0 bar g, such as preferably 3.5-5.5 bar g. Preferably, the method may further comprise that the operating pressure of the second concentration column is above the operating pressure of the first concentration column. The operating pressure interval here provided relates to the preferred pressure within the column (i.e. independently of whether measured at the top or at the bottom).

[0106] The method may further comprise the steps of providing a second condensate stream from the second concentration column and transferring at least a portion of the excess heat energy of the second condensate stream to at least one of i) the first raw product stream, ii) the first condensate stream from the first concentration column and iii) the stabilizer column. The method may further comprise the steps of feeding a second low pressure steam stream to the fourth reboiler and providing a second steam condensate stream from said fourth reboiler, and transferring at least a portion of the excess heat energy of the second steam condensate stream to at least one of i) the first raw product stream, ii) the first condensate stream from the first concentration column and iii) the stabilizer column.

[0107] The method may further comprise feeding a pure product stream to the first compressor for injection cooling. Preferably, the method further comprises feeding to the compressor i) a portion of the sixth product stream provided from the drum, optionally provided to the first compressor via a pump, ii) a second portion of said seventh product stream, iii) a pure product stream from storage such as from a product storage tank or any combination thereof for injection cooling.

[0108] A method for producing a chemical product stream

[0109] Provided is also a method for producing a chemical product stream, in a chemical plant as disclosed herein, wherein said method comprises: feeding a first syngas stream to a product synthesis section to output a first raw product stream, feeding at least a portion of said first raw product stream to said system for distillation to output a product stream such as a seventh product stream.

[0110] The method may further comprise that the first raw product stream is a raw methanol stream, and the seventh product stream is a first distilled methanol stream.

[0111] Additionally, or alternatively, wherein said plant further comprises a carbon source feed and further comprises a reformer section, said method further comprises: feeding the carbon source feed to the reformer section to provide a syngas stream, preferably, providing from the reformer section at least a portion of the first syngas stream.

[0112] Additionally, or alternatively, wherein the chemical plant comprises a first H2O feed and an e- syngas section comprising at least one SOEC for electrolysis of H2O, the method further comprises: feeding the first H2O feed to the e-syngas section comprising at least one SOEC for electrolysis of H2O to provide a second hydrogen steam, and admixing at least a portion of said second hydrogen stream with one or more stream(s) comprising carbon monoxide / carbon dioxide to provide the first syngas stream. Additionally, wherein the system for distillation further comprises a third portion of the third product stream, the method further comprises: indirectly transferring heat energy from the third portion of the third product stream to the first H2O feed via heat exchange, or wherein the chemical plant further comprises an electrolysis evaporator, the method further comprises: feeding a water feed and the third portion of the third product stream to the electrolysis evaporator, indirectly transferring heat energy from the third portion of the third product stream to the water feed and / or to the boiling water comprised in the electrolysis evaporator so as to evaporate water to evaporator steam and output the first H2O feed.

[0113] Suitably, wherein the chemical plant further comprises an electrolysis evaporator, the temperature of third portion of the third product stream received by said electrolysis evaporator is above the temperature of the evaporator steam. Preferably, the third portion of the third product stream is of a temperature of 160 °C or above, and the electrolysis steam is of a temperature of between 100-160 °C such as 148 °C.

[0114] Additionally, or alternatively, the chemical plant may comprise a first carbon dioxide feed and an e-syngas section comprising at least one SOEC for electrolysis of carbon dioxide, and the method further comprises: feeding the first carbon dioxide feed to the e-syngas section comprising at least one SOEC for electrolysis of carbon dioxide to provide a second carbon monoxide stream, admixing at least a portion of said second carbon monoxide stream with one or more stream(s) comprising hydrogen / carbon dioxide to provide the first syngas stream.

[0115] Additionally, or alternatively, the chemical plant comprises a second carbon dioxide feed and a carbon capture unit, and the method further comprises: feeding the second carbon dioxide feed to the carbon capture unit to provide the second carbon dioxide stream, and admixing at least a portion of said second carbon dioxide stream with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream.

[0116] Specifically, wherein the chemical plant further comprises the system for distillation further comprising a fourth portion of the third product stream, the method comprises: indirectly transferring heat energy from the fourth portion of the third product stream to the carbon capture unit and / or the second carbon dioxide feed via heat exchange, or wherein the carbon capture unit further comprises a stripper reboiler, wherein the stripper reboiler further comprises a CCh-rich liquid, the method further comprises feeding the fourth portion of the third product stream to the stripper reboiler, indirectly transferring heat energy from the fourth portion of the third product stream to the CC -rich liquid comprised in the stripper reboiler so as to release CO2 gas and provide the second carbon dioxides stream.

[0117] Suitably, the temperature of the fourth portion of the third product stream fed to said stripper reboiler is above the temperature of the CCh-rich liquid comprised in the stripper reboiler. Preferably, the fourth portion of the third product stream fed to said stripper reboiler is of a temperature of 110-150 °C, and the CC -rich liquid comprised in the stripper reboiler is of a temperature of 100-130 °C.

[0118] A method for district heating

[0119] Provided is further a method for district heating, wherein said arrangement for district heating is as disclosed herein, wherein said method comprises: indirectly transferring heat energy from the fifth portion of the third product stream to the district heating grid such as to the at least one district heating stream via heat exchange.

[0120] Suitably, the temperature of the fifth portion of the third product stream is above the temperature of the least one district heating stream. Preferably, the temperature of the fifth portion of the third product stream is of equal to or above 110 °C, and the temperature of the least one district heating stream is between 50-100 °C.

[0121] Specific embodiments

[0122] Figure 1 shows a first schematic drawing of the system (200) for distillation. The system (200) comprises: a first raw product stream (1); a stabilizer section (10); a first concentration column (20); a first heat exchanger (30), a second heat exchanger (30 '); a first compressor (40); a first reboiler (50) and a second reboiler (80); a drum (60); and a first pump (70). The stabilizer section (10) is arranged to receive the first raw product stream (1) and provide a second raw product stream (11) and a first off-gas stream (12). The first concentration column (20) is arranged to receive the second raw product stream (11) and distil said stream (11) so as to output a first product steam (21), a first condensate stream (29), and optionally a second off-stream (22). The first heat exchanger (30) is arranged to receive at least a first portion (21a) of the first product stream (21) and to output a second product stream (31). The first compressor (40) is arranged to receive at least a second portion (21b) of the first product stream (21) and to output a third product stream (41). The first reboiler (50) is arranged to receive at least a first portion (41a) of the third product stream (41) and provide heat energy to the first concentration column (20), and wherein at least a portion of the heat energy for the first reboiler (50) is provided from the third product stream (41) such that said first reboiler (50) outputs a fourth product stream (51). The fourth product stream (51) is arranged to be fed to the inlet of the second heat exchanger (30') so as to output a fifth product stream (32). The drum (60) is arranged to receive at least a portion of the second product stream (31) and at least a portion of the fifth product stream (32) and provide a sixth product stream (61). The first pump (70) is arranged to receive at least a portion of the sixth product stream (61) from the drum (60) and output a seventh product stream (71), optionally wherein a portion (71a) of said seventh product stream (71) is fed to the first concentration column (20). Finally, the second reboiler (80) is arranged to provide additional heat energy to the first concentration column (20).

[0123] Specifically, the first reboiler (50) is a side-drawn reboiler such that said first reboiler (50) receives a first take-off stream (23) from the first concentration column (20) and provides a first return stream (24), arranged to be fed to the first concentration column (20). The second reboiler (80) is arranged to provide heat energy to the bottom of the first concentration column (20), wherein said second reboiler (80) receives a second take-off stream (25) from the first concentration column (20) and provides a second return stream (26), arranged to be fed to the first concentration column (20).

[0124] The system may further comprise a pure product stream (61a, 71b, 72) arranged to provide injection cooling in the first compressor (40). Hence, the first compressor (40) may further be arranged to receive a pure product stream (61a, 71b, 72), wherein the pure product stream is arranged to provide injection cooling. Preferably, the pure product stream (61a, 71b, 72) arranged to be received by the first compressor comprises i) a portion (61a) of the sixth product stream (61) provided from the drum (60), optionally provided to the first compressor via a pump (pump not shown on Fig.), ii) a second portion (71b) of said seventh product stream (71), iii) a pure product stream from storage (72) such as from a product storage tank or any combination thereof.

[0125] For the method of distillation, where the first raw product stream comprises methanol, the first product stream (21) is suitably approx. 68 °C, the first portion (41a) has a saturation temperature of in the interval 100-140 °C. This system may further include heat integration designs, preferably arranged to transfer heat from the first condensate stream (29). For the method of distillation, where the first raw product stream comprises methanol, the first condensate stream (29) is approx. 120-130 °C.

[0126] Figure 2 shows a second schematic drawing of the system for distillation comprising units and streams as comprised in Figure 1 and further comprising that the stabilizer column (10a) is arranged to receive heat energy from a second portion (41b) of the third product stream (41). Specifically, the system further comprises a third reboiler (15), wherein the third reboiler is arranged to receive a fourth take-off stream (14) and provide a fourth return stream (16). At least a portion of the heat energy of the second portion (41b) of the third product stream (41) is arranged to be transferred to the fourth take-off stream (14). The third reboiler is arranged to output a cooled second portion (17) of the third product stream. At least a portion of the cooled second portion (17) of the third product stream is arranged to be fed to the inlet of a third heat exchanger (30"), and the third heat exchanger (30") is arranged to provide an additional product feed (33) to the drum. This arrangement may provide sufficient energy to the stabilizer column (10a) to drive the purification process within said stabilisation column (10a) such that no additional energy needs to be provide to the stabilizer column (10a).

[0127] Figure 3 shows a third schematic drawing of the system for distillation comprising units and streams as comprised in Figure 1 and 2, however with the difference that the first reboiler (50) and the second reboiler (80) are arranged to provide heat energy to the bottom of the first concentration column (20). More specifically, the third take-off stream (27) is split in a first stream (27a) comprising a first portion of the third take-off stream (27) and a second stream (27b) comprising a second portion of the third take-off stream (27). The first reboiler (50) is arranged to receive the first stream (27a) and outputs a third stream (28a) comprising vaporised product and the second reboiler (80) is arranged to receive the second stream (27b) and outputs a fourth stream (28b) comprising vaporised product. The first concentration column is then arranged to receive the third stream (28a) and the fourth stream (28b) as combined stream fed to the first concentration column as the third return stream (28).

[0128] In addition, the second reboiler the second reboiler (80) is arranged to receive a first low pressure steam stream (2) and output a first steam condensate stream (82). The excess heat energy of the first steam condensate stream (82) may be arranged to be transferred by heat exchange (not shown on Figure) to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), and iii) the stabilizer column (10a) as reboiling heat, preferably to the stabilizer column (10a) as reboiling heat. Figure 4 shows a fourth schematic drawing of the system for distillation comprising units and streams as comprised in Figure 3, however with the difference that the second reboiler (80) is arranged to receive heat energy from least a portion (91a) of an eighth product stream (91) provided from a second concentration column (90). More specifically, the system for distillation further comprises a second concentration column (90), a second drum (100), a second pump (110), and a fourth reboiler (120). The second concentration column (90) is arranged to receive at least a portion of the first condensate stream (29) and provide an eighth product stream (91), a second condensate stream (94), and a third off-stream (92). The second reboiler (80) is arranged to receive at least a portion (91a) of the eighth product stream (91) to output a ninth product stream (81). The second drum (100) is arranged to receive at least a portion of said ninth product stream (81) and output a tenth product stream (101), and the second pump (110) is arranged to receive at least a portion of the tenth product stream (101) and provide an eleventh product stream (111). A first portion (Illa) of the eleventh product stream (111) is arranged to be fed as a feed to the second concentration column (90), and optionally, a second portion (111b) of the eleventh product stream (111) is arranged to be combined with at least a portion of said seventh product stream (71), hereby providing a product stream (150).

[0129] The fourth reboiler (120) is arranged to provide the necessary heat energy to the second concentration column (90) to drive the distillation process. The fourth reboiler (120) is arranged to provide heat energy to the bottom of the second concentration column (90). Specifically, the fourth reboiler (120) is arranged to receive at least a portion of a fifth takeoff stream (93) and provide a fifth return stream (121), wherein at least a portion of the fifth return stream (121) is arranged to be fed to the second concentration column (90). Additionally, the fourth reboiler is arranged to receive a second low pressure steam stream (3) and output a second steam condensate stream (122). In this way, the fourth reboiler may be arranged to transfer heat energy from the second low pressure steam stream (3) to the bottom of the second concentration column (90).

[0130] For the method of distillation, where the first raw product stream comprises methanol, the first product stream (21) is suitably approx. 68 °C, the first portion (41a) and second portion (41b) of the third product stream (41) has a saturation temperature of between 100-120 °C. This system may further include heat integration designs, preferably arranged to transfer heat energy from second condensate stream (94). The second steam condensate stream (122) may be approx. 170 °C. The second condensate stream is arranged to transfer heat to the first condensate stream such to cool the second condensate stream to 110-130 °C followed by additional heat energy transfer to the first raw product stream (1) (Heat integration not shown on Figure).

[0131] Figure 5 shows a fifth schematic drawing of the system for distillation comprising units and streams as comprised in Figure 2, however here specified that the second reboiler (80) is arranged to receive heat energy from least a portion (91a) of an eighth product stream (91) provided from a second concentration column (90). In this way, the system for distillation further comprises a second concentration column (90), a second drum (100), a second pump (110), a fourth reboiler (120), and a second low pressure steam stream (3) and all streams arrangements between these units / stream (90, 100, 110, 120, 3) are as described for Figure 4.

[0132] Figure 6 shows a first schematic drawing of a chemical plant (350). Specifically, the chemical plant comprises a first syngas stream (311), a product synthesis section (320), the system for distillation according to the system disclosed herein (200). The product synthesis section (320) is arranged to receive the first syngas stream and output a first raw product stream (1), and the system for distillation (200) is arranged to receive at least a portion of said first raw product stream (1) from said product synthesis section (320) and output a product stream (150, 71, 111b). Specifically, the product synthesis section (320) may be a methanol synthesis section (320a).

[0133] The chemical plant may further comprise a first H2O feed (301) and an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O, wherein the e-syngas section is arranged to receive the first H2O feed (301) and output a second hydrogen steam (312), preferably wherein at least a portion of said second hydrogen stream (312) is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream (311).

[0134] The chemical plant comprising an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O, may further comprise an electrolysis evaporator (308). Said chemical plant may further comprise that the system for distillation (200) further comprises a third portion (41c) of the third product stream (41). Specifically, the electrolysis evaporator (308) may be arranged to receive a water feed (301a) and output the first H2O feed (301), and further be arranged to receive at least a portion of the third portion (41c) of the third product stream (41) and output a condensed third portion of the third product stream (341c). More specifically, the electrolysis evaporator (308) may be arranged to receive a water feed (301a), comprise boiling water, and output the first H2O feed (301), wherein the boiling water comprised in the electrolysis evaporator is arranged to receive heat energy from the third portion (41c) of the third product stream (41). In this way, the electrolysis evaporator (308) allows for indirect transfer of heat energy from the third portion (41c) of the third product stream (41) to the boiling water comprised in the electrolysis evaporator (308) so as to evaporate water to evaporator steam and output the first H2O feed (301).

[0135] The chemical plant may further comprises a first carbon dioxide feed (302) and an e-syngas section (310) comprising at least one SOEC for electrolysis of carbon dioxide, wherein the e- syngas section (310) is arranged to receive the first carbon dioxide feed (302) and output a second carbon monoxide stream (312'), preferably wherein at least a portion of said second carbon monoxide stream (312') is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon dioxide to provide the first syngas stream (311).

[0136] The chemical plant comprising an e-syngas section (310) comprising at least one SOEC for electrolysis of carbon dioxide, may further comprise a heat exchanger (308'). Said chemical plant may further comprise that the system for distillation (200) further comprises a third portion (41c) of the third product stream (41). Specifically, the heat exchanger (308') may be arranged to receive a cold carbon dioxide feed (301b) and output the first carbon dioxide feed (302), and further be arranged to receive at least a portion of the third portion (41c) of the third product stream (41) and output a condensed third portion of the third product stream (341c'). In this way, the heat exchanger (308') allows for indirect transfer of heat energy from the third portion (41c) of the third product stream (41) to the cold carbon dioxide feed (301b) so as to heat carbon dioxide and output the first carbon dioxide feed (302).

[0137] In this way, all of the third portion (41c) of the third product stream (41) may be arranged to be received by the electrolysis evaporator (308), or all of the third portion (41c) of the third product stream (41) may be arranged to be received by the heat exchanger (308'), or alternatively a portion of the third portion (41c) of the third product stream (41) may be arranged to be received by the electrolysis evaporator (308) and / or a portion of the third portion (41c) of the third product stream (41) may be arranged to be received by the heat exchanger (308').

[0138] The chemical plant may further comprise a first H2O feed (301), a first carbon dioxide feed (302) and an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O and carbon dioxide, wherein the e-syngas section is arranged to receive the first H2O feed (301) and the first carbon dioxide feed (302) and output a syngas stream.

[0139] The chemical may plant further comprise a second carbon dioxide feed (314) and a carbon capture unit (315), wherein the carbon capture unit (315) is arranged to receive the second carbon dioxide feed (314) and output a second carbon dioxide stream (317), preferably wherein at least a portion of said second carbon dioxide stream (317) is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream (311).

[0140] The chemical plant comprising a carbon capture unit (315), may further comprise that the system for distillation (200) further comprises a fourth portion (41d) of the third product stream (41). Specifically, the carbon capture unit (315) may be arranged to receive a second carbon dioxide feed (314) and output the second carbon dioxide stream (317), and further be arranged to receive at least a portion of the fourth portion (41d) of the third product stream (41) and output a condensed fourth portion of the third product stream (341d). More specifically, said carbon capture unit may further comprise a stripper reboiler and the stripper reboiler may further comprises a CCh-rich liquid. Said stripper reboiler may be arranged to receive at least a portion of the fourth portion (41d) of the third product stream (41), indirectly transfer heat energy from the fourth portion (41d) of the third product stream (41) to the CCh-rich liquid comprised in the stripper reboiler so as to output the second carbon dioxide stream (317) and a condensed fourth portion of the third product stream (341d). In this way, the carbon capture unit (315), preferably specifically the stripper reboiler may be arranged to receive heat energy from a fourth portion (41d) of the third product stream (41) via heat exchange.

[0141] Figure 6 further shows a first schematic drawing of an arrangement for district heating (350 combined with 400), said arrangement comprising a district heating grid (335, 342) comprising at least one district heating stream (335), and the chemical plant (350) comprising the system for distillation (200). The system for distillation (200) further comprises a fifth portion (41e) of the third product stream (41), wherein the district heating grid such as the at least one district heating stream (335) is arranged to receive heat energy from a fifth portion (41e) of the third product stream (41) via heat exchange. Specifically, a heat exchanger (340) may be arranged to receive at least a portion of the fifth portion (41e) of the third product stream (41) and at least one district heating stream (335) and to output at least one heated district heating stream (342) and a condensed, fifth portion (41e) of the third product stream (41).

[0142] Figure 7 shows a first schematic drawing of a chemical plant (300). Specifically, the chemical plant comprises: a H2O rich-feed (301); a CC -rich feed (302); an e-syngas section (310); a product synthesis section (320); the system (200) for distillation. The e-syngas section (310) is arranged to receive said H2O rich-feed (301) and said CC -rich feed (302), and output a syngas stream (311). The product synthesis section (320) is arranged to receive at least a portion of said syngas stream (311) and output a first raw product stream (1). The product synthesis section (320) may be a methanol synthesis section (320a). The system for distillation (200) is arranged to receive said first raw product stream (1) from said product synthesis section (320) and provide a product stream (150, 71, 111b). Additionally, heat integration designs may also be included from elsewhere in the chemical plant so as from outside the system for distillation (Not shown on Figure). Specially, the e- syngas section (310) and / or the product synthesis section (320, 320a) may be arranged to provide additional heat energy to at least one of i) the first raw product stream (1), ii) the stabilizer column (10a), iii) the first condensate stream (29) from the first concentration column (20), optionally iv) the second concentration column (90) and optionally the fourth reboiler (120), such as through heat exchange.

[0143] EXAMPLE 1

[0144] The following examples are calculated on the basis of the production of 300 metric tonnes methanol per day. The experiments show that the total steam consumption (i.e. amount of steam needed from outside the system for distillation) is significantly reduced when applying heat integration and is then further reduced when applying vapor recompression (i.e. heat pump). The largest decrease in steam consumption is observed when including the vapor recompression (i.e. heat pump). Experiment 1 changes from 1.64 to 0.34 kg steam / kg methanol, and experiment 2 changes from 1.22 to 0.29 kg steam / kg methanol. In comparison, a typical chemical synthesis of methanol based on e-syngas generates less than 1.0 kg steam / kg methanol. Therefore, the invention has the potential to balance the steam generation and steam consumption. The power for the compressor can suitably come from production of renewable electrical power production.

Claims

CLAIMS1. A system (200) for distillation, said system (200) comprising : a first raw product stream (1); a stabilizer section (10) comprising a stabilizer column (10a); a first concentration column (20); a first heat exchanger (30), optionally a second heat exchanger (30 '); a first compressor (40); a first reboiler (50) and a second reboiler (80); a drum (60); a first pump (70); wherein the stabilizer section (10) is arranged to receive the first raw product stream (1) and provide a second raw product stream (11), and a first off-gas stream (12); wherein the first concentration column (20) is arranged to receive the second raw product stream (11) and distil said stream (11) so as to output a first product steam (21), a first condensate stream (29), and optionally a second off-stream (22); wherein the first heat exchanger (30) is arranged to receive at least a first portion (21a) of the first product stream (21) and to output a second product stream (31); wherein the first compressor (40) is arranged to receive at least a second portion (21b) of the first product stream (21) and to output a third product stream (41); wherein the first reboiler (50) is arranged to receive at least a first portion (41a) of the third product stream (41) and provide heat energy to the first concentration column (20), and wherein at least a portion of the heat energy for the first reboiler (50) is provided from the third product stream (41) such that said first reboiler (50) outputs a fourth product stream (51); wherein the fourth product stream (51) is arranged to be fed to the inlet of the first heat exchanger (30) together with the first portion (21a) of the first product stream (21), and / or the fourth product stream (51) is arranged to be fed to the inlet of the second heat exchanger (30') so as to output a fifth product stream (32);wherein the drum (60) is arranged to receive at least a portion of the second product stream (31) and / or at least a portion of the fifth product stream (32) and provide a sixth product stream (61); wherein the first pump (70) is arranged to receive at least a portion of the sixth product stream (61) from the drum (60) and output a seventh product stream (71), optionally wherein a portion (71a) of said seventh product stream (71) is fed to the first concentration column (20); wherein the second reboiler (80) is arranged to provide additional heat energy to the first concentration column (20).

2. The system according to claim 1, wherein the first raw product stream (1) is a raw methanol stream, and the seventh product stream (71) is a first distilled methanol stream.

3. The system according to any one of the preceding claims, wherein the first reboiler (50) is a side-drawn reboiler such that said first reboiler (50) receives a first take-off stream (23) from the first concentration column (20) and provides a first return stream (24), arranged to be fed to the first concentration column (20).

4. The system according to any one of claims 1-2, wherein the first reboiler (50) is arranged to provide heat energy to at least a portion of the second raw product stream (11) from the stabilizer section (10).

5. The system according to any one of the preceding claims, wherein the second reboiler (80) is arranged to provide heat energy to the bottom of the first concentration column (20), wherein said second reboiler (80) receives a second take-off stream (25) from the first concentration column (20) and provides a second return stream (26), arranged to be fed to the first concentration column (20).

6. The system according to any one of claims 1-2, wherein the first reboiler (50) and the second reboiler (80) are arranged to provide heat energy to the bottom of the first concentration column (20), preferably wherein at least one of the first and / or second reboiler receives at least a portion of a third take-off stream (27) and such that the first reboiler is arranged to receive heat from the first portion (41a) of the third product stream (41) and wherein the first and / or second reboiler is arranged to provide at least one third return stream (28) to the first concentration column (20).

7. The system according to any one of the preceding claims, wherein the stabilizer column (10a) is arranged to receive heat energy from a second portion (41b) of the third product stream (41), preferably said system further comprises a third reboiler (15), wherein said third reboiler is arranged to receive a fourth take-off stream (14) and provide a fourth return stream (16), and wherein at least a portion of the heat energy of the second portion (41b) of the third product stream (41) is arranged to be transferred to the fourth take-off stream (14).

8. The system according to any one of the preceding claims, wherein at least a portion of the excess heat energy of the first condensate stream (29) from the first concentration column (20) is arranged to be transferred by heat exchange to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), and iii) the stabilizer column (10a) as reboiling heat, preferably to the i) the first raw product stream (1) and / or ii) the second raw product stream (11).

9. The system according to any one of the preceding claims, wherein the second reboiler (80) is arranged to receive a first low pressure steam stream (2) and output a first steam condensate stream (82), and wherein excess heat energy of the first steam condensate stream (82) is arranged to be transferred by heat exchange to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), and iii) the stabilizer column (10a) as reboiling heat, preferably to the stabilizer column (10a) as reboiling heat.

10. The system according to any one of claims 1-8, wherein said system further comprises a second concentration column (90), a second drum (100), a second pump (110), and a fourth reboiler (120) and wherein said second concentration column (90) is arranged to receive at least a portion of the first condensate stream (29) and provide an eighth product stream (91), a second condensate stream (94), and a third off-stream (92), and wherein said fourth reboiler (120) is arranged to provide heat energy to the second concentration column (90), wherein the second reboiler (80) is arranged to receive at least a portion (91a) of the eighth product stream (91) to output a ninth product stream (81), wherein said second drum (100) is arranged to receive at least a portion of said ninth product stream (81) and output a tenth product stream (101), and wherein said second pump (110) is arranged to receive at least a portion of the tenth product stream (101) and provide an eleventh product stream (111), wherein a first portion (Illa) of said eleventh product stream (111) is arranged to be fed as a feed to the second concentration column (90), and optionally, wherein a second portion (111b) of said eleventh product stream (111) is arranged to be combined with at least a portion of said seventh product stream (71).

11. The system according to claim 10, wherein the fourth reboiler (120) is arranged to provide heat energy to the bottom of the second concentration column (90), preferably wherein the fourth reboiler (120) is arranged to receive at least a portion of a fifth take-off stream (93) and provide a fifth return stream (121), wherein at least a portion of the fifth return stream (121) is arranged to be fed to the second concentration column (90).

12. The system according to any one of claims 10-11, wherein at least a portion of the excess heat energy of the second condensate stream (94) is arranged to be transferred by heat exchange to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), iii) the first condensate stream (29) from the first concentration column (20) and iv) the stabilizer column (10a) as reboiling heat, preferably to the first condensate stream (29) and / or the first raw product stream (1).

13. The system according to any one of claims 10-12, wherein the fourth reboiler (120) is arranged to receive a second low pressure steam stream (3) and output a second steam condensate stream (122), and optionally, wherein excess heat energy of the second steam condensate stream (122) is arranged to be transferred by heat exchange to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), iii) the first condensate stream (29) from the first concentration column (20) and iv) the stabilizer column (10a) as reboiling heat, preferably the stabilizer column (10a).

14. The system according to any one of the preceding claims, wherein the stabilizer section (10) further comprises an internal first vapor stream, an internal condenser heat exchanger, an internal drum, and an internal pump, and wherein the stabilizer column (10a) is arranged to provide the internal first vapor stream directly from the top of the column (10a), the excess heat energy of the internal first vapor stream is arranged to be transferred to the first raw product stream (1) by heat exchange.

15. The system according to any one of the preceding claims, wherein the first compressor (40) is further arranged to receive a pure product stream (61a, 71b, 72), wherein the pure product stream is arranged to provide injection cooling.

16. The system according to claim 15, wherein the pure product stream (61a, 71b, 72) arranged to be received by the first compressor comprises i) a portion (61a) of the sixth product stream (61) provided from the drum (60), optionally provided to the first compressor via a pump, ii) a second portion (71b) of said seventh product stream (71), iii) a pure product stream from storage (72) such as from a product storage tank or any combination thereof.

17. A chemical plant (350) is provided, said chemical plant comprising : a first syngas stream (311); a product synthesis section (320); the system for distillation (200) according to the system disclosed herein, wherein said product synthesis section (320) is arranged to receive the first syngas stream and output a first raw product stream (1), and wherein said system for distillation (200) is arranged to receive at least a portion of said first raw product stream (1) from said product synthesis section (320) and output a product stream (150, 71, 111b) such as a seventh product stream (71).

18. The chemical plant (350) according to claim 17, wherein said plant further comprises a carbon source feed and further comprises a reformer section, wherein the reformer section is arranged to receive the carbon source feed and output a syngas stream, preferably said reformer section is arranged to output at least a portion of the first syngas stream (311).

19. The chemical plant (350) according to any one of claims 17-18, wherein said plant further comprises a first H2O feed (301) and an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O, wherein the e-syngas section (310) is arranged to receive the first H2O feed (301) and output a second hydrogen steam (312), preferably wherein at least a portion of said second hydrogen stream (312) is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream (311).

20. The chemical plant (350) according to any one of claims 17-19, wherein said plant further comprises a first carbon dioxide feed (302) and an e-syngas section (310) comprising at least one SOEC for electrolysis of carbon dioxide (CO2), wherein the e-syngas section (310) is arranged to receive the first carbon dioxide feed (302) and output a second carbon monoxide stream (312'), preferably wherein at least a portion of said second carbon monoxide stream (312') is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon dioxide to provide the first syngas stream (311).

21. The chemical plant (350) according to any one of claims 17-20, wherein said plant further comprises a second carbon dioxide feed (314) and a carbon capture unit (315), wherein the carbon capture unit (315) is arranged to receive the second carbon dioxide feed (314) and output a second carbon dioxide stream (317), preferably wherein at least a portion of said second carbon dioxide stream (317) is arranged to be admixed with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream (311).

22. The chemical plant (350, 300) according to claim 17, the chemical plant comprising : a H2O rich-feed (301); a CC -rich feed (302); an e-syngas section (310); a product synthesis section (320); the system for distillation according to any one of claims 1-14 (200), wherein said e-syngas section (310) is arranged to receive said H2O rich-feed (301) and said CCh-rich feed (302), and output a syngas stream (311), said product synthesis section (320) is arranged to receive at least a portion of said syngas stream (311) and output a first raw product stream (1), and wherein said system for distillation (200) is arranged to receive said first raw product stream (1) from said product synthesis section (320), wherein the e-syngas section (310) and / or the product synthesis section (320) is / are arranged to provide additional heat energy to at least one of i) the first raw product stream (1), ii) the stabilizer column (10a), iii) the first condensate stream (29) from the first concentration column (20), optionally iv) the second concentration column (90) and optionally the fourth reboiler (120), such as through heat exchange.

23. The chemical plant (350) according to claims 17-22, being a methanol plant, said methanol plant comprising a methanol synthesis section (320a), said methanol synthesis section (320a) being arranged to receive a syngas stream (311) and output the seventh product stream (71).

24. The chemical plant (350) according to any one of claims 17-23, wherein the chemical plant comprises an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O and the system for distillation (200) further comprises a third portion (41c) of the third product stream (41), wherein the e-syngas section (310) is arranged to receive the first H2O feed (301) and output a second hydrogen stream (312), wherein the first H2O feed (301) is arranged to receive heat energy from a third portion (41c) of the third product stream (41) via heat exchange.

25. The chemical plant (350) according to any one of claims 17-23, wherein the chemical plant comprises an e-syngas section (310), an electrolysis evaporator (308), and the system for distillation (200) further comprises a third portion (41c) of the third product stream (41), wherein the e-syngas section (310) is arranged to receive a first H2O feed (301), and wherein the electrolysis evaporator (308) is arranged to receive a water feed (301a), comprise boiling water, and output the first H2O feed (301), wherein the boiling water comprised in theelectrolysis evaporator, the water feed (301a) and / or the first H2O feed (301) is arranged to receive heat energy from the third portion (41c) of the third product stream (41).

26. The chemical plant (350) according to any one of claims 17-25, wherein the chemical plant comprises a carbon capture unit (315) arranged to receive a second carbon dioxide feed (314) and the system for distillation (200) further comprises a fourth portion (41d) of the third product stream (41), and wherein the carbon capture unit (315) and / or the second carbon dioxide feed (314) is arranged to receive heat energy from a fourth portion (41d) of the third product stream (41) via heat exchange.

27. An arrangement for district heating (350 combined with 400), said arrangement comprising : a district heating grid (335, 342) comprising at least one district heating stream (335), and the chemical plant (350) comprising the system for distillation (200), wherein the system for distillation (200) further comprises a fifth portion (41e) of the third product stream (41), wherein the district heating grid (335, 342) such as the at least one district heating stream (335) is arranged to receive heat energy from a fifth portion (41e) of the third product stream (41) via heat exchange.

28. A method for distillation of a first raw product stream (1), wherein said system is according to any one of claims 1-15, wherein said method comprises: feeding a first raw product stream (1) to the stabilizer section (10) and providing a second raw product stream (11), and a first off-gas stream (12); feeding at least a portion of the second raw product stream (11) to the first concentration column (20), distilling said stream (11) and providing a first vaporised product steam (21) from said first concentration column (20), a first condensate stream (29), and optionally a second off-stream (22); feeding at least a first portion (21a) of the first product stream (21) to the first heat exchanger (30), and providing a second product stream (31) from said first heat exchanger (30); feeding at least a second portion (21b) of the first product stream (21) to the first compressor (40), and providing a third product stream (41) from the first compressor (40); feeding at least a first portion (41a) of the third product stream (41) to the first reboiler (50), and hereby providing heat to the first concentration column (20), wherein the step of providing heat to the first concentration column (20) comprisesproviding heat energy from the at least first portion (41a) of the third product stream (41) to the first reboiler (50) and providing a fourth product stream (51) from said first reboiler (50); feeding at least a portion of the fourth product stream (51) to the inlet of the first heat exchanger (30) together with the first portion (21a) of the first product stream (21), and / or feeding at least a portion of the fourth product stream (51) to the inlet of the second heat exchanger (30') and providing a fifth product stream (32); feeding at least a portion of the second product stream (31) and / or at least a portion of the fifth product stream (32) to the drum (60), and providing a sixth product stream (61), feeding at least a portion of the sixth product stream (61) from drum (60) to the first pump (70), and providing a seventh product stream (71), and optionally feeding a portion (71a) of said seventh product stream (71) as a fed to the first concentration column (20); providing addition heat energy to the first concentration column (20) by heat energy transfer from the second reboiler (80).

29. The method according to claim 28, wherein the operating pressure of the first concentration column (20) is between 0.1-10.0 bar g, preferably 0.1-1.5 bar g.

30. The method according to any one of claims 28-29, wherein the method further comprises transferring using heat exchange at least a portion of the excess heat energy of the first condensate stream (29) to at least one of i) the first raw product stream (1), ii) the second raw product stream (11) from the stabilizer section (10), and iii) the stabilizer column (10a) as reboiling heat.

31. The method according to any one of claims 28-30, wherein said system is according to any one of claims 10-14, and wherein said method further comprises: feeding at least a portion of the first condensate stream (29) from the first concentration column (20) to the second concentration column (90) and providing an eighth product stream (91) and a third off-stream (92); providing heat energy to the second concentration column (90) by heat energy transfer from the fourth reboiler (120); feeding at least a portion (91a) of the eighth product stream (91) to the second reboiler (80) and providing a ninth product stream (81);feeding at least a portion of said ninth product stream (81) to the second drum (100) and providing a tenth product stream (101); feeding at least a portion of the tenth product stream (101) to the second pump (110) and providing an eleventh product stream (111); feeding a first portion (Illa) of said eleventh product stream (111) as a feed to the second concentration column (90), and optionally, combining a second portion (111b) of said eleventh product stream (111) with at least a portion of said seventh product stream (71).

32. The method according to claim 31, wherein the operating pressure of the second concentration column (90) is between 2.5-10.0 bar g such as preferably between 2.5-7.0 bar g, such as preferably 3.5-5.5 bar g.

33. The method according to any one of claims 31-32, wherein said method further comprises providing a second condensate stream (94) from the second concentration column (90) and transferring at least a portion of the excess heat energy of the second condensate stream (94) to at least one of i) the first raw product stream (1), ii) the first condensate stream (29) from the first concentration column (20) and iii) the stabilizer column (10a).

34. The method according to any one of claims 31-33, wherein said method further comprises feeding a second low pressure steam stream (3) to the fourth reboiler (120) and providing a second steam condensate stream (122) from said fourth reboiler (120), and transferring at least a portion of the excess heat energy of the second steam condensate stream (122) to at least one of i) the first raw product stream (1), ii) the first condensate stream (29) from the first concentration column (20) and iii) the stabilizer column (10a).

35. The method according to any one of claims 28-34, wherein the first portion (41a) of the third product stream (41) has a saturation temperature of more than 3 °C above the temperature of the first or third return streams (24, 28) to the first concentration column (20), such as between 5-20 °C, preferably between 10-15 °C above the temperature of said first or third return streams (24, 28).

36. The method according to any one of claims 28-35, wherein method further comprises the step of feeding a pure product stream (61a, 71b, 72) to the first compressor (40) for injection cooling.

37. A method for producing a chemical product stream, in a chemical plant (350) according to any one of claims 17-26, wherein said method comprises:feeding a first syngas stream (311) to a product synthesis section (320) to output a first raw product stream (1), feeding at least a portion of said first raw product stream (1) to said system for distillation (200) to output a product stream (150, 71, 111b) such as a seventh product stream (71).

38. The method according to claim 37, wherein the first raw product stream (1) is a raw methanol stream, and the seventh product stream (71) is a first distilled methanol stream.

39. The method according to any one of claims 37-38, wherein said plant further comprises a carbon source feed and further comprises a reformer section, and wherein said method further comprises: feeding the carbon source feed to the reformer section to provide a syngas stream, preferably, providing from the reformer section at least a portion of the first syngas stream.

40. The method according to any one of claims 37-39, wherein the chemical plant (350) comprises a first H2O feed (301) and an e-syngas section (310) comprising at least one SOEC for electrolysis of H2O, the method further comprises: feeding the first H2O feed (301) to the e-syngas section (310) comprising at least one SOEC for electrolysis of H2O to provide a second hydrogen steam (312), and admixing at least a portion of said second hydrogen stream (312) with one or more stream(s) comprising carbon monoxide / carbon dioxide to provide the first syngas stream (311).

41. The method according to claim 40, wherein the system for distillation (200) further comprises a third portion (41c) of the third product stream (41), the method further comprises: indirectly transferring heat energy from the third portion (41c) of the third product stream (41) to the first H2O feed (301) via heat exchange, or wherein the chemical plant further comprises an electrolysis evaporator (308), the method further comprises: feeding a water feed (301a) and the third portion (41c) of the third product stream (41) to the electrolysis evaporator (308), indirectly transferring heat energy from the third portion (41c) of the third product stream (41) to the water feed (301a) and / or to the boiling water comprised in the electrolysis evaporator so as to evaporate water to evaporator steam and output the first H2O feed (301).

42. The method according to claim 41, wherein the chemical plant (350) comprises an electrolysis evaporator (308), the temperature of third portion (41c) of the third product stream (41) received by said electrolysis evaporator (308) is above the temperature of the evaporator steam, preferably the third portion (41c) of the third product stream (41) is of a temperature of 160 °C or above, and the electrolysis steam is of a temperature of between 100-160 °C such as 148 °C.

43. The method according to any one of claims 37-42, wherein the chemical plant (350) comprises a first carbon dioxide feed (302) and an e-syngas section (310) comprising at least one SOEC for electrolysis of carbon dioxide, and the method further comprises: feeding the first carbon dioxide feed (302) to the e-syngas section (310) comprising at least one SOEC for electrolysis of carbon dioxide to provide a second carbon monoxide stream (312'), admixing at least a portion of said second carbon monoxide stream (312') with one or more stream(s) comprising hydrogen / carbon dioxide to provide the first syngas stream (311).

44. The method according to any one of claims 37-43, wherein the chemical plant (350) comprises a second carbon dioxide feed (314) and a carbon capture unit (315), and the method further comprises: feeding the second carbon dioxide feed (314) to the carbon capture unit (315) to provide the second carbon dioxide stream (317), and admixing at least a portion of said second carbon dioxide stream (317) with one or more stream(s) comprising hydrogen / carbon monoxide to provide the first syngas stream (311).

45. The method according to claim 44, wherein the chemical plant (350) further comprises the system for distillation (200) further comprising a fourth portion (41d) of the third product stream (41), the method comprises: indirectly transferring heat energy from the fourth portion (41d) of the third product stream (41) to the carbon capture unit (315) and / or the second carbon dioxide feed (314) via heat exchange, or wherein the carbon capture unit (315) further comprises a stripper reboiler, wherein the stripper reboiler further comprises a CC -rich liquid, the method further comprises feeding the fourth portion (41e) of the third product stream (41) to the stripper reboiler, indirectly transferring heat energy from the fourth portion (41d) of the third product stream (41) to the CC -rich liquid comprised in the stripper reboiler so as to release CO2 gas and provide the second carbon dioxides stream (317).

46. The method according to claim 45, wherein the temperature of the fourth portion (41d) of the third product stream (41) fed to said stripper reboiler is above the temperature of the CCh-rich liquid comprised in the stripper reboiler, and preferably, the fourth portion (41d) of the third product stream (41) fed to said stripper reboiler is of a temperature of 110-150 °C, and the CC -rich liquid comprised in the stripper reboiler is of a temperature of 100-130 °C.

47. A method for district heating, wherein said arrangement for district heating (350 combined with 400) is according to claim 27, wherein said method comprises: indirectly transferring heat energy from the fifth portion (41e) of the third product stream (41) to the district heating grid (335, 342) such as to the at least one district heating stream (335) via heat exchange.

48. The method according to claim 47, wherein the temperature of the fifth portion (41e) of the third product stream (41) is above the temperature of the least one district heating stream (335), and preferably the temperature of the fifth portion (41e) of the third product stream (41) is of equal to or above 110 °C, and the temperature of the least one district heating stream (335) is between 50-100 °C.

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