瑞士专利CH703488B1 Combined evaporation / stripping / absorption module.

专利PDF首页>>瑞士专利

专利附录

专利说明

权利要求

类似技术

同族专利

引用文献

法律状态

优先权

专利摘要:
In one process, a portion of a stream of liquid mixture is vaporized to produce a vapor and a depleted liquid stream. The vapor is introduced into a brine capable of exothermic absorption of one or more components from the vapor, and heat is withdrawn to produce at least one heat stream and one brine stream enriched in one or more components. The previously extracted heat is transferred to effect evaporation. This heat transfer is associated with a change of a working fluid from the gaseous to a liquid state. The heat removal involves the conversion of the working fluid from the liquid to the gaseous state. In the liquid state, the working fluid flows only through one or more of gravity, convection and wicking. In the gaseous state, the working fluid flows only through one or more of diffusion and convection.
公开号:CH703488B1
申请号:CH01826/11
申请日:2010-04-16
公开日:2016-10-14
发明作者:Mcgregor Ian；H Belchers Christopher
申请人:Drystill Holdings Inc；
IPC主号:

专利说明:

Field of invention
The present invention relates generally to the field of fluid separation.
Background of the invention
In the field of fluid separation, it is known to use a brine, such as a LiBr brine, for the absorption of a process steam and for the subsequent heat generation. It is also known to use a pump to lead a heat-transporting fluid through a heat exchange circuit in order to lead the heat generated by the absorber to an evaporator or boiler for the generation of the process steam.
Summary of the invention
A method of application to a liquid mixture that is separable by evaporation into a vapor stream and a stream of depleted liquid forms one aspect of the invention. The method comprises: an evaporation step in which a portion of the liquid mixture is evaporated to form the vapor stream and the stream of depleted liquid; an absorption stage in which (i) the steam stream is introduced into a brine stream capable of exothermically absorbing one or more components from the steam, and (ii) heat is withdrawn to produce at least one heat stream and one brine stream which in which one or more components is enriched; and a heat exchange stage in which the heat extracted in the absorption stage is transferred to cause evaporation in the evaporation stage. The heat transfer to cause evaporation is accompanied by the phase change of a working fluid from a gaseous state to a liquid state. The extraction of heat in the absorption stage comprises the phase change of the working fluid from the liquid state to the gaseous state. In the liquid state, the working fluid flows only by one or more of gravity, convection, and wicking.
In the gaseous state, the working fluid flows only through one or more of diffusion and convection.
Another aspect of the invention relates to the use of a device for performing the above. Procedure. The device is for use with a stream of a liquid mixture which is separable by evaporation into a vapor stream and a depleted stream of liquid. The apparatus includes an arrangement which, in use: defines a first volume in which the liquid mixture is received and separated into the vapor stream and the stream of depleted liquid; • defines a first liquid passage through which the depleted stream exits the first volume; • defines a steam passage through which the steam flow exits the first volume; • defines a second volume into which the steam passage opens; • comprises a heat and mass transfer device which is at least partially arranged in the second volume, the heat and mass transfer device: (i) receiving a stream of brine which is capable of exothermic absorption of one or more components from the steam; (ii) introducing the stream of brine into the steam; and (iii) removing heat from the second volume to produce at least one heat flow and one flow of brine that is enriched in the one or more components; • defines a second liquid passage through which the brine stream, which is enriched with respect to the one or more components, leaves the second volume; and • comprises heat exchange means for transferring the heat flow to effect the separation in the first volume.
During operation of the device, the heat transfer into the first volume is accompanied by the phase change of a working fluid from a gaseous state to a liquid state; the extraction of heat from the first volume comprises the phase change of the working fluid from the liquid state to the gaseous state; in the liquid state, the working fluid flows only by one or more of gravity, convection, and wicking; and in the gaseous state, the working fluid only flows through one or more of diffusion and convection.
According to another aspect of the invention, the heat transport device and part of the heat and mass transport device can be defined by one or more heating tubes, each of the one or more heating tubes having a heat-absorbing part, which is arranged in the second volume, and a Has heat releasing part which is arranged in the first volume to effect the heat transfer.
According to another aspect of the invention, the one or more heating tubes can be arranged so that the part of the heating tubes that is in the first volume acts when it is used as a packed evaporation column, and the part of the heating tubes that is in the second volume acts as a packed absorption column.
According to another aspect of the invention, the vapor leaving the first volume can be in operation essentially in a vapor-liquid equilibrium with the liquid mixture entering the first volume.
According to another aspect of the invention, the temperature of the depleted liquid stream leaving the first volume can be lower than the temperature of the liquid mixture entering the first volume during operation.
According to another aspect of the invention, the pressure in the first volume and the temperature of the liquid mixture entering the first volume during operation can be such that essentially all of the heat transferred from the first volume leads to the evaporation of the liquid mixture.
According to another aspect of the invention: the arrangement can also define an exhaust opening leading into the first volume; and during operation, at least a substantial portion of the steam can be absorbed in the second volume, the remaining portion leaving the second volume through the vent.
According to another aspect of the invention, the device can also comprise a desorption device for receiving the brine flow which is generated by the heat and mass transfer device and which generates: the flow of brine which is used for exothermic absorption of the one or more components is capable of steam; and a product stream.
According to another aspect of the invention, the device can also comprise: a secondary absorber which, during operation: (i) absorbs the remainder of the steam; and (ii) introducing the remainder of the steam into a secondary stream of brine capable of exothermic absorption of the one or more components to produce a dilute brine.
According to another aspect of the invention, the desorption device can also take up the diluted brine and also generate the secondary brine flow.
According to another aspect of the invention, the pressures in the first volume and in the second volume can be reduced compared to atmospheric pressure during operation; at least a major part of the vapor can be absorbed in the second volume; and a vacuum pump can effect removal of at least a portion of the non-condensables of the vapor from the device.
According to another aspect of the invention, the first volume can be defined by one or more first cavities and the second volume by one or more second cavities.
According to another aspect of the invention, each of the one or more first cavities and each of the one or more second cavities can be defined in a respective container; and a pipe joint may define the vapor passage.
According to another aspect of the invention, each of the one or more first cavities and each of the one or more second cavities can be defined in a container.
According to another aspect of the invention, a pipe connection arranged outside the container can form the steam passage.
According to another aspect of the invention: the container can be divided by partitions to define one or more of the first cavities and one or more of the second cavities; one or more openings formed in the partition walls can represent the vapor passage.The device can form part of a bioproduct manufacturing plant, which is another aspect of the invention. In addition to the device, the system includes an arrangement in which the catabolism of a broth (translator's note: i.e. stillage or mash) occurs on a continuous basis during operation. The apparatus is connected to the plant for withdrawing a broth stream on a continuous basis, removing a degradation inhibitor from the withdrawn broth to generate an inhibitor-containing stream and a residual stream, and returning the residual stream to the plant.
According to another aspect of the invention, the degradation can be fermentation and the inhibitor can be alcohol.
According to another aspect of the invention, the inhibitor-containing stream can contain a higher concentration of inhibitor than the broth.
According to another aspect of the invention, a withdrawal stream of the broth can be drawn off during operation in order to avoid toxin build-up; the exhaust stream can be fermented in batches; and the plant may further comprise a further device which receives the product of a batch fermentation and (i) produces a stream of total distillate from which ethanol is substantially removed and a (ii) ethanol-enriched broth which is fed to the desorption device and separated becomes.
According to another embodiment of the invention, when used: the broth withdrawn from the system can have temperatures of 28 ° C. to 32 ° C. and an ethanol concentration of 4% to 10%; the remainder of the stream may have a temperature 2 ° C to 4 ° C lower than the withdrawn stream and an ethanol concentration which is 2% to 6% lower than that of the withdrawn stream; and the pressure in the first volume can be about 40-133 mbar.
According to another aspect of the invention, when used: the broth withdrawn from the plant can have a temperature of about 30 ° C. and an ethanol concentration of about 7%; the remainder of the stream can have a temperature of about 28 ° C and an ethanol concentration of about 2%; the pressure in the first volume can be 40 bar.
According to another aspect of the invention, the heating pipes can be arranged parallel to a common axis and the system can be designed to pivot about a horizontal axis which is arranged perpendicular to the common axis.
According to yet another aspect of the invention, the device according to the invention can be part of a bioproduct manufacturing plant which has an arrangement in which, when using the batch-wise breakdown of a broth takes place. In this system, the device is coupled to the arrangement in order to draw off a broth stream, to remove a degradation inhibitor from the broth withdrawn in order to generate a stream containing inhibitor and a residual stream, and to feed the residual stream back into the arrangement.
Further advantages, features and characteristics of the present invention emerge from the following detailed description and the attached drawings, which are briefly described below, it being understood that the same transfer symbols in the drawings also denote the same structures throughout. 1 is a schematic view of a stripping / absorption module according to an embodiment of the invention; Fig. 2 is a schematic view of the module of Fig. 1 in an example of use; Figure 3 is a view similar to Figure 2 of another example of use of the arrangement of Figure 1; Fig. 4 is another schematic view of another embodiment of the arrangement of Fig. 1; Figure 5 is a schematic view of an ethanol production plant employing two modules according to Figure 1; FIG. 6 is a simplified schematic view of the ethanol production plant of FIG. 5 in combination with a simplified representation of the arrangement of FIG. 4; Figure 7 is a schematic view of another embodiment of the module of Figure 1; Figure 8 is a schematic illustration of another aspect of the module of Figure 1; and FIG. 9 is a cross-sectional view of another embodiment of the module of FIG. 1.
Detailed description
In Fig. 1, a stripping / absorption module (SAM) is shown in a schematic representation and denoted by the general transfer number 20.
The module comprises: a container 21, a pair of partition walls 22, 24, a plurality of heating tubes 26 and a pair of manifolds 28, 30.
The container 21 is a sturdy container suitable for operation at reduced pressures, e.g. 30 torr is suitable.
The pair of dividers includes a first divider 22 and a second divider 24. The first divider 22 extends up from the base of the container and terminates below the top of the container. The second partition wall 24 is spaced from the first, extends downward from the top of the container and ends above the base. By this arrangement, the first cavity 32 and the second cavity 34 are defined within the container and are connected to one another by a conduit 35 which is defined by the space between the partitions 22,24.
The container is pierced by a plurality of inlets 36-44, a lower inlet 36, 38 at the base of each cavity and an upper inlet 40, 42 adjacent the top of each cavity, and an uppermost inlet 44 near the top of the second cavity 34.
The plurality of heating tubes 26 extend from the first cavity 32 into the second cavity 34 and are used to transfer heat from the second cavity 34 into the first cavity 32. The heating tubes 26 are of conventional design and are not described in further detail here. The pair of distributors 28, 30 each extend from the upper inlets 40, 42 of the first and second cavities 32, 34 and are designed to wet the heating tubes 26.
From this it is understood that the main functional features of the illustrated SAM are as follows:• first cavity 32;• second cavity 34;• the line 35, which connects the first with the second cavity;• the lower inlets 36, 38;• the upper inlets 40, 42;The top inlet 44;• the heating tubes 26; and• the distributors 28, 30.
Fig. 2, which is a schematic embodiment of an exemplary separator for use with a stream of mixed liquid which can be separated into a vapor stream and a depleted liquid stream by evaporation, shows the manner in which these essential functional features are shown in FIG Operation.
It can be seen here that the module 20 is shown together with a second absorber 46 and a desorption device 48.
First of all, with respect to the module 20, it is understood that the first cavity 32 forms a first volume. There the stream of mixed liquid is received and partially evaporated to form the aforementioned steam and depleted liquid streams. The implementation of the evaporation is explained below in the description relating to the heating pipes.
The lower inlet 42 at the base of the first volume defines a first liquid passage through which the depleted liquid flow leaves the first volume 32.
The line 35 forms a second volume in which the steam passage 35 opens.
The uppermost outlet 44 forms an exhaust opening.
The distributors 28, 30 and the heating tubes 26 together form the heat and mass transfer device and the heat exchange device. The heat and mass transfer device: (i) receives a stream of brine capable of exothermic absorption of one or more components from the steam; (ii) introduces the brine stream into the steam (i.e., the brine is sprayed or dripped onto the heating tubes 26 in the second volume 34); and (iii) extracting heat from the second volume to produce at least one heat flow and a brine flow that is enriched in one or more components. The heat exchange means transfers the heat flow into the first volume 32 to provide such a separation, and each of the heating tubes 26 as such has a heat receiving part located in the second volume and a heat releasing part located in the first volume .
The brine can e.g. consist solely of a LiBr solution which has a lithium bromide substance concentration between 40% and 70%, preferably between 45% and 65%. However, any absorbent fluid known in the art would be suitable.
The lower inlet 38 at the base of the second volume 34 forms a second liquid passage through which the brine stream enriched with respect to one or more components leaves the second volume 34.
As a result of the use of the heating tubes, it is understood that the heat transfer into the first volume is accompanied by a phase change of a working fluid, in this case water, from a gaseous to a liquid state; the extraction of heat from the second volume comprises the evaporation of the working fluid from the liquid state to the gaseous state; the working fluid in the liquid state flows only by gravity and / or wicking; and the working fluid in this gaseous state flows only by diffusion and / or convection. Working fluids other than water could and would be used, depending on the application: Ammonia and commercially available cooling system fluids are only two examples. The selection of the working fluid is a measure that is customary for specialists and is therefore not described here.
The heating tubes 26 are stacked so that the part of the heating tubes located in the first volume 32 acts as a packed evaporation column in operation and the part of the heating tubes located in the second volume 34 operates as a packed absorption column.
Accordingly, it follows that the vapor leaving the first volume 32 is essentially in vapor-liquid equilibrium with the mixed liquid entering the first volume 32; • At least a substantial portion of the vapor is absorbed in the second volume 34, with the remainder exiting the second volume through the vent 44.
The secondary absorber 46: (i) absorbs the remainder of the steam, i. E. the part not absorbed in the SAM; and (ii) introducing the remainder of the steam into a second brine stream capable of exothermic absorption of the one or more components. This produces a dilute brine and also a gas stream composed of non-absorbent gases and non-absorbed absorbent components, the latter being discharged from the secondary absorber in the direction of arrow 50.
The desorption device 48, i. a boiler or a distillation system, receives the brine flow generated in the heat and mass exchange device and the dilute brine generated by the secondary absorber 46 and generates: the flow of the brine 52, which is capable of exothermic absorption of at least one or more components from the steam and the secondary brine stream 54, and • a product stream 56.
Fig. 3 shows a modification of the structure shown in Fig. 2 for use under conditions in which the pressures in the first volume and in the second volume are reduced relative to atmospheric pressure. In this application, at least the majority of the enriched steam is absorbed in the second volume, and a vacuum pump 58 supplies the non-condensable portions and any non-absorbed condensable portions of the steam to be discharged from the system.
Fig. 4 is intended to be an illustration of the schematic of a plant which could be suitable for use in concentrating apple juice. This plant is generally similar to that of FIG. 3, ie it comprises a SAM 20, a second absorber 46 and a vacuum pump 58, but the desorption device 48 can comprise a two-stage desorber instead of a distillation device (since the purpose in this application is not the Fractionating the mixed liquid, but merely concentrating the juice is). The two-stage desorber comprises a number of heat exchangers 60 for exchanging heat between the various parts of the process, a pair of boilers 62 and various pumps 64. Predictions have been made regarding the operation of this system, the values of which are shown in Table 1 below.
The predicted heat input (in the form of 125 psig steam) injected by stream 12 is 557 Btu / lb of evaporated water. This compares favorably with a simple evaporation efficiency (about 1000 Btu / lb). At the same time, in view of the schematic representation, experts can expect that the system is relatively inexpensive to build and operate.
[0054] FIG. 5 is understood to be a schematic representation of an ethanol production plant, which comprises: a grain milling device 66, a cooking / liquefaction device 68 and a saccharification device 70; these parts are all essentially conventional in that they receive grain and produce a feed suitable for fermentation; A yeast conditioner 72, for generating a stream of water, enzymes and yeast; A continuous agitation reactor tank (CSTR) 76: this is where the feed, water, etc. are introduced, fermentation being continuous and where a drain 135 is withdrawn; A SAM device 20 connected to the CSTR for continuously withdrawing a stream of fermentation broth, preferably to remove alcohol from the withdrawn broth and an alcohol-enriched (brine) stream 104 and a residual stream 131 and recycle the residual stream 131 into the CSTR 76; • a batch tank 78, which receives the discharge stream 135 in batches and ferments; A second SAM device 20 connected to receive from batch tank 78 and (i) generating a stream of total distillate from which ethanol is substantially removed and (ii) generating an ethanol enriched brine; • a distillate processor 79 (control shutdown); A secondary absorber 46 for absorbing the remaining portion of the absorbent portions that have not been absorbed by the SAM device 20; An exhaust air scrubber 74 for extracting traces of alcohol, among other things from the batch tank 78, and a secondary absorber 46 for recirculation into the cooking device 68 before the non-condensable components are released to the atmosphere via the stream 142; • three desorbers 84, 82, 80, which are arranged to form a three-stage desorber, for the regeneration of the brine and generation of a concentrated ethanol stream as well as for the generation of a recycled water stream; A cooler 90 and a storage container 92 for receiving the stream of recycled water and returning it to the grain grinding device 68; • a rectification / dehydration device 86; • heat exchangers 60 and pumps 64 for transferring the flows between the various elements; and the ethanol product storage device 88.
Expected operating conditions for the various streams given in Table 2:
A person skilled in the art will readily understand how the device in question is to be operated with these currents and the schematic representation. Accordingly, a detailed, point-by-point description is not required and is not given for the sake of brevity.
However, Table 2 is noteworthy at least for the following: The product streams fed to the rectifier 86 have concentrations suitable for conventional processing by pervaporation or molecular sieve methods; • Calculations suggest that high quality heating requirements, i.e. a fuel generated heat for which high pressure desorber is 844,717 BTU / gallon ethanol generated (through rectifier 86); this differs advantageously from conventional ethanol production plants in which the heat requirements up to rectification can be up to 18,000 BTU / gallon, • the broth withdrawn from the CSTR 76 has a temperature of around 30 ° C and the remaining broth has a temperature of around 28 ° C; these conditions are advantageous in that the broth never reaches a temperature greater than about 30 ° C (or supercooled) which could damage the living yeast.
Again, it can be deduced that the system can be built relatively inexpensively, which is apparent to specialists.
Without wishing to be bound by theory, it is believed that these beneficial energy and construction cost requirements result in part from the fact that the pressure in the first volume 32 and the temperature of the mixed liquid entering the first volume 32 are such that substantially the any heat transferred into the first volume results in vaporization of the mixed liquid; • the temperature of the rest of the broth is lower than that of the broth withdrawn, which reduces the cost of cooling the CSTR; • a multi-effect desorption is used and • the cooling loads associated with the evaporation are relatively moderate (with the evaporation in areas where very cold cooling water is not abundant, i.e., as is usually the case, must be generated by mechanical means).
Fig. 6 shows a simplified modification of the structure of Fig. 5 with further details with regard to advantageous methods of distillate processing using a SAM according to the invention.
Briefly, the CSTR 76 receives the feed 96 and produces strong beer 98 which is fed to a SAM system 20. Schwachbier 100 is returned from this SAM to the CSTR 76. A withdrawal stream is returned to the batch tank 78. Strong beer 102 from batch tank 78 is directed to its own SAM 20. The total distillate 108 from the batch tank 78 is centrifuged at 110 to produce a wet cake 112 and a dilute distillate 114, the latter being fed to another SAM 20 to produce a syrup 116 which, along with the cake 112, is in a DDGS dryer 180 is dried. The dilute brine 120 produced by each of the SAMs is fed to the distillation plant 94 for regeneration. Although the distillation plant 94 shows that all diluted brine fractions converge, it goes without saying that the distillation plant 94 can be designed in two parts, so that separate brine flows with a relatively higher concentration of ethanol and brine flows with relatively low ethanol fractions can be kept separate from one another.
The predicted benefits with respect to the above predicted examples have been verified experimentally.
Test results
Twenty heating tubes, each 178 mm (7.0 ") long and 1 mm (0.25") in diameter, were placed horizontally one above the other to form arrays approximately 25.4 mm (10.0 ") high. This structure was sandwiched between transparent acrylic sheets. Two separate, adjacent chambers (an evaporator chamber and an absorber chamber) were formed between the sheets, with the heating tubes running through both chambers. A 12.5 mm (0.5 inch) inner diameter hose was used to connect the head of the evaporator chamber to the foot of the absorber chamber. A crude fluid manifold was placed at the top of each chamber. A two liter flask in communication with the atmosphere was placed at the top of each chamber and connected to the liquid manifold of that chamber through a flow control valve. At the foot of each chamber an outlet for liquid was provided which was connected to a collection flask. An outlet at the top of the absorber chamber was connected to a standard laboratory vacuum pump which was provided with two traps to protect against water and ethanol vapor.
A first level of protection was a secondary absorber which was partially filled with a strong cold LiBr solution. Gases on the way to the vacuum pump were bubbled through the solution in the flask and thereby freed of absorbent components. The second level of protection was a cold trap fed with liquid nitrogen.
Two runs were made. For each run, measured quantities of brine were placed in the washing bottle and the flask connected to the absorber and a measured amount of beer was added to the flask connected to the evaporator; the flow control valve was opened and the temperature and pressure of the fluids passed through the system were measured. The readings were stopped when either or both of the feed flasks were emptied.
Wash bottle initial weightFinal weight 1303 g1304 g cold trap initial weightFinal weight 00 beer initial weightFinal weight 83 g ethanol + 952 g water = 1035 g (8% EtOH)70 g ethanol + 931 g water = 1000 g (7% EtOH) brine initial weightFinal weight 701 g water + 1052 g LiBr = 1753 g (60% LiBr)13 g ethanol + 713 H2O + 1052 LiBr = 1778 (59% LiBr)
The test confirmed that the SAM is able to preferentially remove ethanol from an ethanol-water mixture and at the same time to cool the ethanol-water mixture. It also shows that a secondary absorber is a useful way to remove residual water and ethanol vapor from the vacuum section. The coefficient of heat exchange of the device for this run was calculated to be 33 BTU / hr / ft 2 / ° F.
Wash bottle initial weight final weight 1303 g1304 g cold trap initial weight final weight 016.5 g ethanol + 16.5 g water = 33 g (50% EtOH) beer initial weight final weight 481 g ethanol + 1236 g water = 1717 g (28% EtOH)307 g ethanol + 1154 g water = 1462 g (21% EtOH) brine initial weight final weight 1239 g water + 1859 g LiBr = 3098 g (60% LiBr)115 g ethanol + 1293 g H2O + 1859 g LiBr = 3267 (43% LiBr)
This test also confirms that the SAM system can preferentially remove ethanol from an ethanol-water mixture and at the same time cool the ethanol-water mixture. The heat exchange coefficient of the device in this run was calculated to be 70 BTU / hr / ft 2 / ° F. Since the liquid distribution system in the test facility left a considerable part of the surface area of the heating pipes unwetted, this performance is considered to be relatively cheap. It is expected that a more thorough liquid distribution will bring the coefficient into agreement with the values published for commercial systems, typically in excess of 150 BTU / hr / ft 2 / ° F.
Although Figure 1 shows a schematic representation of a SAM, it will be apparent to those skilled in the art that changes can be made.
7 shows such a possibility, namely an arrangement in which the heating tubes 26 are arranged parallel to a common axis X-X, and that this structure is capable of a pivoting movement about a horizontal axis Y-Y which is perpendicular runs to the common axis. It is believed that this arrangement could be used to effect periodic removal of liquid from the heat emitting portions of the tubes.
FIG. 8 shows another possibility in which the first volume 32 could be formed by one or more first cavities 32A, the second volume 34 by one or more second cavities 34A, each of the first or more first cavities 32 and each of the one or more second cavities 34A could be formed by a respective container 130, with the tubes 132 defining the vapor passage 36. It is expected that this embodiment could have some benefit in terms of reduced construction costs as well as heat exchange efficiency (shorter tubes are usually better). Separate containers make it possible to generate considerable pressure differentials and correspondingly larger temperature differentials between absorption and evaporation. A larger temperature differential would lead to a higher heat transfer through the heating pipes. This could have advantages in terms of cost of capital, i. fewer heating pipes and smaller containers.
It goes without saying, however, that lower pressure differentials could even be achieved with a SAM system of the type shown schematically in FIG. 1, for example by interposing a pump or a fan in the vapor passage.
9 shows a further possible SAM structure in which the container 21 is formed by a horizontally arranged cylindrical container, the steam passage 35 (shown by the arrows A) is formed by an external pipe connection (not shown) and that first volume 32 and second volume 34 are separated from one another by a vertical forked wall 140. The wall is formed by upper ridges 142 and lower ridges 144 which extend outwardly from the tubular wall of the container 21. Between ridges 142 and 144, a rubber sheet 148 is sandwiched between steel sheets 146 and 150 which are connected to one another by upper brackets 156 and lower brackets 152. The rubber sheet 148 is perforated with holes so that the heating tubes 26 can be passed through in a practically tight state; the steel sheets 146, 150 have corresponding holes of larger diameter in order to allow free passage of the heating pipes. Without being limited to any particular theory, it is believed that this arrangement is advantageous from the standpoint of relatively low construction costs and ease of maintenance. For maintenance, the operator would only have to remove one end of the container and pull out the entire heating pipe arrangement horizontally. If desired, different bearings or rollers (not shown) could also be used to further simplify the construction. Although only a single bifurcated wall is shown, the container could be divided by two walls, with the heating tubes extending through each wall to create a structure with functionality similar to that shown in FIG. In this (not shown) embodiment with two walls, the heating tubes could be arranged at an angle so that a flow of droplets could be generated forwards and backwards in the chamber.
Although specific operating conditions have been set forth in the description with reference to FIGS. 4 and 5, it should be understood that numerous modifications are possible.
For example, in connection with an ethanol production plant in which the viability of the yeast is to be maintained with continuous fermentation, at least the following aspects can be considered advantageous: The broth withdrawn from the fermentation plant can have a temperature of about 28 ° C to 32 ° C ° C and an ethanol concentration of about 4% to 10%; • The residual broth can have a temperature that is around 2 ° C to 4 ° C lower than that of the withdrawn broth, and an ethanol concentration that is around 2% to 4% lower than that of the withdrawn broth, and • a Pressure in the first volume of about 30 to 100 torr.
Further, while the structure of Figure 5 is described herein as being useful for ethanol production, those skilled in the art will readily understand that the structure could be used to perform other separations, particularly, but not limited to, butanol and methanol. Furthermore, the general structure of Figure 5 could be useful for any degradation reaction that uses a degradation inhibitor that can be removed by absorption. Furthermore, although the description refers to continuous production, this is not absolutely necessary. In the case of batch ethanol production, broth could be withdrawn from the batch tank while fermentation is in progress and passed through a SAM system to withdraw ethanol. Removing ethanol from the batch would relieve the yeast and could reduce cycle time and increase yield. While in connection with ethanol and a LiBr brine, the thermodynamic parameters are kept so that preferably ethanol is withdrawn, i.e. with a higher concentration than in the total mass, this is not absolutely necessary. In connection with an aqueous system in which, for example, water and a further component are withdrawn, there would be the possibility that water would be withdrawn in preference to the other component and that supplementary water would be added to balance the flows. In this regard it is further to be understood that in the description and in the following claims "liquid mixture" means a liquid mixed with another material, which other material may be liquid, such as alcohol, but that this is not necessary, such as among others the apple juice concentrator example shows.

权利要求:
Claims (26)
[1]
A method for application to a stream of a liquid mixture which is separated by evaporation into a vapor stream and an enriched stream of the liquid, comprising: I an evaporation step in which a portion of the stream of liquid mixture is evaporated to the vapor stream and the produce depleted stream of the liquid; II an absorption stage, in which (i) the steam flow is introduced into a brine flow which is capable of exothermic absorption of one or more components from the steam and (ii) heat is extracted in order to generate at least one heat flow and one brine flow which in Relation to which one or more components is enriched; and III a heat exchange stage in which the heat extracted in the absorption stage is transferred to cause evaporation in the evaporation stage, where α the heat transfer for causing evaporation is accompanied by the phase transition of a working fluid from a gaseous to a liquid state; β the extraction of heat in the absorption stage comprises the phase transition of the working fluid from the liquid state to the gaseous state; σ the working fluid flows in the liquid state only by gravity and / or convection and / or wicking; and γ the working fluid in the gaseous state flows only by diffusion and / or convection.
[2]
2. The method of claim 1 using an apparatus comprising A comprises a first volume in which the liquid mixture is received and separated into the vapor stream and the depleted stream of liquid, A1 comprises a first liquid passage through which the depleted stream is the first Exits volume, A2 comprises a vapor pass through which the vapor stream exits the first volume; B comprises a second volume in which the steam passage opens; the B1 comprises heat and mass transfer devices which are at least partially arranged in the second volume, the heat and mass transfer devices (i) receiving a brine flow and being able to exothermically absorb one or more components from the steam; (ii) introducing the brine stream into the steam; and (iii) extracting heat from the second volume to generate at least one heat flow and a brine flow which is enriched with respect to the one or more components, B2 comprises a second liquid passage through which the brine flow, which is with respect to the one or more a plurality of components is enriched, leaves the second volume and C comprises a heat transport device for transferring the heat flow into the first volume to effect the separation, wherein a the heat transfer into the first volume is accompanied by a phase change of a working fluid from a gaseous state to a liquid state ; b the extraction of heat from the second volume comprises the phase transition of the working fluid from the liquid state to the gas state; c the working fluid in the liquid state only flows by gravity and / or convection and / or wicking and the working fluid in the gaseous state flows only by diffusion and / or convection.
[3]
3. The method according to claim 2, wherein the heat transport device and part of the heat and mass transfer device of the device used are formed by one or more heating tubes, each of the one or more heating tubes having a heat-absorbing part which is arranged in the second volume , and a heat emitting portion disposed in the first volume to effect the heat transfer.
[4]
4. The method according to claim 3, in which the one or more heating tubes of the device used are stacked so that the part of the heating tubes in the first volume when used as a packed evaporation column and the part of the heating tubes in the second volume when used as a packed absorption column .
[5]
5. The method according to claim 3, wherein the heating tubes of the device used are arranged parallel to a common axis and the parallel heating tubes are capable of pivoting movement about a horizontal axis which is oriented perpendicular to the common axis.
[6]
6. The method according to any one of claims 2 to 5, wherein the device further comprises an outlet leading from the second volume; so that at least a substantial part of the vapor is absorbed in the second volume and the remainder leaves the second volume through the outlet.
[7]
7. The method according to claim 6, wherein the device used further comprises a desorption device for receiving the brine flow which is formed by the heat and mass transfer device, and a brine flow which is capable of exothermic absorption of the one or more components from the steam, and generates a product stream.
[8]
8. The method of claim 7, wherein the device used further comprises a secondary absorber which (i) absorbs the remainder of the steam and (ii) introduces the remainder of the steam into a secondary brine stream which is capable of exothermically absorbing the one or more components to create a dilute brine.
[9]
9. The method according to claim 8, in which the desorption device of the device used receives the diluted brine and generates the secondary brine flow.
[10]
10. The method according to any one of claims 2 to 9, wherein the first volume of the device used are formed by one or more first cavities and the second volume by one or more second cavities.
[11]
11. The method of claim 10, wherein each of the one or more first cavities and each of the one or more second cavities of the device used are each formed by a container and the vapor passage is formed by pipes.
[12]
12. The method of claim 11, wherein each of the one or more first cavities and each of the one or more second cavities of the device used is formed by a container.
[13]
13. The method according to claim 12, wherein the tubes of the device used form the vapor passage outside the container.
[14]
14. The method of claim 13, wherein (i) the container of the apparatus used is partitioned by partitions to define the one or more first cavities and the one or more second cavities and (ii) one or more openings in the partitions form the vapor passage.
[15]
15. The method according to any one of claims 1 to 14, wherein the vapor leaving the first volume is essentially in vapor-liquid equilibrium with the liquid mixture entering the first volume.
[16]
16. The method of claim 1 or 15, wherein the temperature of the depleted stream of liquid exiting the first volume is lower than the temperature of the liquid mixture entering the first volume.
[17]
17. The method according to any one of claims 1, 15 or 16, wherein the pressure in the first volume and the temperature of the liquid mixture entering the first volume are such that practically all of the heat transferred into the first volume leads to the evaporation of the liquid mixture .
[18]
18. The method according to any one of claims 1 and 15 to 17, wherein the pressures in the first volume and in the second volume are reduced relative to atmospheric pressure; an at least predominant part of the vapor is absorbed in the second volume, and a vacuum pump removes at least the non-condensable parts of the vapor from the device.
[19]
19. A method for the production of organic products using the method according to any one of claims 2 to 18, in which the device additionally comprises an arrangement for the continuous or batch-wise breakdown of a broth,the arrangement serving to withdraw a stream of brew on a continuous basis or on a batch basis; removing a degradation inhibitor from the withdrawn broth to produce an inhibitor-containing stream and a residual flow, and recycling the residual flow to the assembly.
[20]
20. The method of claim 19, wherein the bioproduct is made by fermentation and the inhibitor is alcohol.
[21]
21. The method of claim 20, wherein the inhibitor-containing stream contains a higher concentration of the inhibitor than the broth.
[22]
22. The method of claim 21, wherein a withdrawal stream of the broth is withdrawn to avoid toxin build-up and the withdrawal stream is fermented in batches, and (i) a stream of total distillate from which ethanol is substantially removed, and (ii) a broth enriched with respect to ethanol, which is fed to the desorption device and separated, is generated.
[23]
23. The method according to any one of claims 20 to 22, wherein the broth withdrawn from the device has a temperature of 28 ° C to 32 ° C and an ethanol concentration of 4% to 10%; the tail stream has a temperature 2 ° C to 4 ° C lower than that of the withdrawn stream and an ethanol concentration that is 2% to 6% lower than that of the withdrawn stream and the pressure in the first volume is about 40 –133 mbar.
[24]
24. The method of claim 23, wherein the broth withdrawn from the device has a temperature of about 30 ° C and an ethanol concentration of about 7%; the remainder of the stream has a temperature of approximately 28 ° C. and an ethanol concentration of approximately 2% and the pressure in the first volume of the device is approximately 40 mbar.
[25]
25. Use of a device for performing the method according to claim 1, wherein the device A comprises a first volume in which the liquid mixture is received and separated into the vapor flow and the depleted flow of the liquid, A1 comprises a first liquid passage through which the depleted stream exits the first volume, A2 comprises a vapor pass through which the vapor stream exits the first volume; B comprises a second volume in which the steam passage opens; the B1 comprises heat and mass transfer devices which are at least partially arranged in the second volume, the heat and mass transfer devices (i) receiving a brine flow and being able to exothermically absorb one or more components from the steam; (ii) introducing the brine stream into the steam; and (iii) extracting heat from the second volume to generate at least one heat flow and a brine flow which is enriched with respect to the one or more components, B2 comprises a second liquid passage through which the brine flow, which is with respect to the one or more a plurality of components is enriched, leaves the second volume and C comprises a heat transport device for transferring the heat flow into the first volume to effect the separation, wherein a the heat transfer into the first volume is accompanied by a phase change of a working fluid from a gaseous state to a liquid state ; b the extraction of heat from the second volume comprises the phase transition of the working fluid from the liquid state to the gas state; c the working fluid in the liquid state only flows by gravity and / or convection and / or wicking and the working fluid in the gaseous state flows only by diffusion and / or convection.
[26]
26. The device for performing the method according to claim 1, wherein the device A comprises a first volume for receiving a liquid mixture and separating it into a vapor stream and a depleted stream of the liquid, A1 comprises a first liquid passage for exiting the depleted stream from the first volume , A2 comprises a steam passage for exiting a steam flow from the first volume, B a second volume for receiving steam from the steam passage (A2); the B1 comprises heat and mass transfer devices which are at least partially arranged in the second volume, the heat and mass transfer devices (i) receiving a brine stream and being able to exothermically absorb one or more components from the steam; (ii) can introduce the brine stream into the steam; and (iii) can withdraw heat from the second volume, B2 comprises a second liquid passage through which the brine flow can leave the second volume and C comprises a heat transport device for transferring the heat flow into the first volume to effect the separation.

类似技术:

公开号 | 公开日 | 专利标题

CH703488B1|2016-10-14|Combined evaporation / stripping / absorption module.

WO2004038031A1|2004-05-06|Apparatus for the production of alcohol

DE10347695A1|2004-05-06|Multi-stage vacuum distillation, vacuum cooling and vacuum freezing processes and apparatus for solution separation and seawater desalination

CN103204776B|2015-03-25|Production method for extracting pyrethrin from pyrethrum flower

EP2089130B1|2019-09-11|Installation for the distillation of alcohol, especially ethyl alcohol, from fermented mash

CN101757802A|2010-06-30|Energy-saving device for low-temperature reduced-pressure extracting and concentrating traditional Chinese medicine

CN105693585A|2016-06-22|System and method for separating N-methylpyrrolidone/chloroform

EP2510101A1|2012-10-17|Method for obtaining ethanol during fermentation

DE102018114366A1|2019-12-19|Process and device for the treatment of biological substances, in particular fermentation residues of plant and animal origin, in particular from biogas plants, of liquid manure or other organic waste products

DE602004002069T2|2007-03-01|Improved process for the production of ethanol from cereals

EP0237520B1|1991-02-27|Process for the production of ethanol from raw materials containing sugar, and installation for carrying out the process

CN205501169U|2016-08-24|System for separation N - methyl 2 pyrrolidone chloroform

WO2010070716A1|2010-06-24|Method of producing ethanol and apparatus therefor

CN205164181U|2016-04-20|Crystal system is evaporated in succession to multiple -effect

DE102018205810A1|2019-10-17|Desorber device for a heat pump

CN111406828B|2022-01-21|Device and process for extracting soybean effective components by using mixed solvent

CN107937226B|2021-06-08|Alcohol distillation system

CN206081735U|2017-04-12|High -efficient circulation extraction system of ionic liquid

WO2021148175A1|2021-07-29|Method for the energy-efficient production of sodium and potassium alcoholates

CN111378521A|2020-07-07|Novel process for leaching grease by actively boosting and reducing pressure

CN202284190U|2012-06-27|Circulatory 1,3-propanediol | treating column used in continuous production process of polytrimethylene terephthalate |

DE1914265C3|1977-02-10|Process for removing gaseous components in the purification of water

DE1122506B|1962-01-25|Process for obtaining pure methyl ethyl ketone

DD260518A1|1988-09-28|METHOD FOR BRUEDENWAER USE IN SUGAR PRODUCTION

DE2050886A1|1971-05-06|Process for the fractionation of a mixture from the cleavage reaction of hydroperoxides

同族专利:

公开号 | 公开日

WO2010121374A1|2010-10-28|

RU2011145431A|2013-05-27|

CA2759409C|2017-05-30|

KR20120007054A|2012-01-19|

CN106215445B|2019-02-22|

EP2421622B1|2017-10-11|

ZA201107716B|2012-09-26|

JP5947715B2|2016-07-06|

EP2421622A1|2012-02-29|

IL215749D0|2012-01-31|

RU2540574C2|2015-02-10|

US8757599B2|2014-06-24|

CN106215445A|2016-12-14|

IL215749A|2016-08-31|

CA2759409A1|2010-10-28|

BRPI1013312A2|2017-05-16|

US20120267079A1|2012-10-25|

CN102405083A|2012-04-04|

US8608841B2|2013-12-17|

CA2663397A1|2010-10-20|

MX340460B|2016-07-08|

AU2010239064B2|2016-03-17|

US20110117633A1|2011-05-19|

AU2010239064A1|2011-11-24|

US20140073044A1|2014-03-13|

KR101772236B1|2017-08-28|

MX2011011013A|2012-02-08|

BRPI1013312B1|2020-03-03|

US9345987B2|2016-05-24|

US20160256796A1|2016-09-08|

US9868076B2|2018-01-16|

JP2012523949A|2012-10-11|

EP2421622A4|2014-06-25|

引用文献:

公开号 | 申请日 | 公开日 | 申请人 | 专利标题

US1461540A|1921-06-09|1923-07-10|Jr Thomas Mee|Electric lantern|

US1461640A|1921-08-15|1923-07-10|Firm Ag Kummler & Matter|Process and apparatus for evaporating liquids|

CH166487A|1932-08-12|1934-01-15|Chem Ind Basel|Process for evaporating liquids.|

US2729564A|1951-03-02|1956-01-03|George J Keller|Method of recovering volatile flavoring oils|

US3480515A|1964-04-03|1969-11-25|Aqua Chem Inc|Method and apparatus for vapor compression distillation and vapor washing of impure water|

US3261766A|1964-12-11|1966-07-19|Fluor Corp|Multistage evaporation with absorption of distilled vapors|

CA931070A|1968-10-24|1973-07-31|A. Hodgson Robert|Gas dehydration process|

US4209364A|1974-04-10|1980-06-24|Rothschild Herbert F|Process of water recovery and removal|

JPS6044033B2|1977-11-07|1985-10-01|Babcock Hitachi Kk|

DE2951557C2|1979-12-21|1984-08-23|Buckau-Walther AG, 4048 Grevenbroich|Method for operating a thermal material separation process with integrated heat recovery and device for carrying out the method|

DE3016406C2|1980-04-29|1985-11-28|Fried. Krupp Gmbh, 4300 Essen|Multi-stage thermal material separation process with a combined vapor compressor and heat transformer to recover the heat contained in the vapors and a device for carrying out the process|

US4309243A|1980-06-05|1982-01-05|Sundquist Charles T|Vertical tube distillers|

SU1011138A1|1982-01-29|1983-04-15|Всесоюзный Научно-Исследовательский И Проектный Институт По Очистке Технологических Газов,Сточных Вод И Использованию Вторичных Энергоресурсов Предприятий Черной Металлургии|Multistep evaporation installation|

US4458500A|1982-06-16|1984-07-10|The United States Of America As Represented By The United States Department Of Energy|Absorption heat pump system|

US4539076A|1982-09-27|1985-09-03|Swain R L Bibb|Vapor compression distillation system|

JPH0124521B2|1984-07-31|1989-05-12|Hitachi Shipbuilding Eng Co|

SU1502038A1|1986-11-17|1989-08-23|Воскресенский филиал Научно-исследовательского института по удобрениям и инсектофунгицидам им.проф.Я.В.Самойлова Научно-производственного объединения "Минудобрения"|Plant for concentrating phosphoric acid|

US4846240A|1987-09-10|1989-07-11|Erickson Donald C|High cop absorption heat pumped evaporation method and apparatus|

US4963231A|1988-06-13|1990-10-16|Ahlstromforetagen Svenska Ab|Method for evaporation of liquids|

US5061306A|1990-05-01|1991-10-29|Cheng Chen Yen|Multiple effect absorption refrigeration processes and apparatuses for use therein|

JPH0571223B2|1990-11-28|1993-10-06|Masanao Hirose|

US5566551A|1994-08-29|1996-10-22|Cheng; Chen-Yen|Vapor pressure enhancement air cooling-heating process and apparatuses for use therein|

US5645694A|1993-03-31|1997-07-08|Vacom Ii, L.P.|Process and apparatus for vapor compression distillation|

US5772850A|1995-05-11|1998-06-30|Morris; Bobby D.|Apparatus for vapor compression distillation|

US5755933A|1995-07-24|1998-05-26|The M. W. Kellogg Company|Partitioned distillation column|

FI106577B|1996-09-04|2001-02-28|Abb Installaatiot Oy|Device for transmitting heating and cooling power|

CN1206622A|1997-04-29|1999-02-03|巴斯福股份公司|Crystal forming by evaporation and steam condensation|

DK173837B1|1999-01-15|2001-12-10|Funki Manura As|Process and apparatus for purifying wastewater|

DE10021624A1|2000-05-04|2001-11-08|Basf Ag|Partition column|

JP3865217B2|2001-12-21|2007-01-10|株式会社ササクラ|Evaporator|

US20040231970A1|2003-05-21|2004-11-25|Lang Chou|Fluid distillation apparatus having improved efficiency|

RU2275224C2|2004-01-21|2006-04-27|Владимир Иванович Бердников|Heat and mass exchange apparatus|

US7390353B2|2005-07-18|2008-06-24|Siemens Power Generation, Inc.|System for removing water from flue gas|

US20090218210A1|2005-10-14|2009-09-03|Laura Demmons|Energy-efficient distillation system|

US7655071B2|2005-12-16|2010-02-02|Shell Oil Company|Process for cooling down a hot flue gas stream|

JP5285860B2|2007-02-21|2013-09-11|エスペック株式会社|Dehumidifier|

CA2663397A1|2009-04-20|2010-10-20|Ian Mcgregor|Stripping absorption module|CA2663397A1|2009-04-20|2010-10-20|Ian Mcgregor|Stripping absorption module|

BR112013005045A2|2010-09-02|2019-09-24|Butamax Tm Advanced Biofuels|method for removing an alcohol product from a fermentation liquid|

US8574406B2|2010-02-09|2013-11-05|Butamax Advanced Biofuels Llc|Process to remove product alcohol from a fermentation by vaporization under vacuum|

EP2683463B1|2011-03-08|2018-05-16|Drystill Holdings Inc.|Process and apparatus for removing heat and water from flue gas|

US9931582B2|2011-03-08|2018-04-03|Drystill Holdings Inc.|Process and apparatus for removing heat and water from flue gas|

BR112014013741A2|2011-12-09|2017-06-13|Butamax Advanced Biofuels Llc|alcohol removal methods, alcohol recovery system, compositions and food|

DE102013215665B4|2013-08-08|2022-01-20|Fraunhofer-Gesellschaft zur Förderung der angewandten Forschung e.V.|Device and method for the production of food products produced by fermentation|

CN107551587B|2017-10-20|2020-10-30|新中天环保股份有限公司|Distillation equipment for recovering organic solvent|

CN112283972A|2020-09-16|2021-01-29|北京建筑大学|Bubbling absorption type lithium bromide absorption heat pump and control method thereof|

法律状态:
2013-12-13| PFA| Name/firm changed|Owner name: DRYSTILL HOLDINGS INC., CA Free format text: FORMER OWNER: DRYSTILL HOLDINGS INC., CA |

优先权:

申请号 | 申请日 | 专利标题

CA2663397A|CA2663397A1|2009-04-20|2009-04-20|Stripping absorption module|

US23141209P| true| 2009-08-05|2009-08-05|

US31315610P| true| 2010-03-12|2010-03-12|

PCT/CA2010/000604|WO2010121374A1|2009-04-20|2010-04-16|Combined vaporizing/stripping absorption module|

[返回顶部]