CN205759801U - Head fraction column system - Google Patents
Head fraction column system Download PDFInfo
- Publication number
- CN205759801U CN205759801U CN201520909226.3U CN201520909226U CN205759801U CN 205759801 U CN205759801 U CN 205759801U CN 201520909226 U CN201520909226 U CN 201520909226U CN 205759801 U CN205759801 U CN 205759801U
- Authority
- CN
- China
- Prior art keywords
- head fraction
- column
- fraction column
- stream
- organic streams
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
This utility model relates to head fraction column system.A kind of process and system reclaimed for acrylonitrile and HCN includes head fraction column system, and it operates into reduction head fraction column condenser duty and minimizing equipment, maintains required purity and specification in the case of the minimum growth of reboiler duty simultaneously.In one aspect, this process includes providing the charging including acrylonitrile, HCN and water to flow to head fraction column；In head fraction column, distill this feed stream produce the head fraction column column overhead stream including HCN and the bottom liquid stream including acrylonitrile；From including that water and sideing stream of organic head fraction column remove effluent；Organic streams is provided from effluent separation at least some water and Organic substance；Organic streams is made to return head fraction column；With adjustment from the ratio of the amount of the effluent removed that sides stream of head fraction column with the amount of the organic streams returning head fraction column in lower section of sideing stream, to provide the HCN of 500ppm or less to bottom liquid stream.
Description
Technical field
Provide a kind of process reclaimed for acrylonitrile and HCN and system.More specifically, head fraction column (heads column) system operates into reduction head fraction column condenser duty, and reduces equipment requirements, increases, with the minimum of reboiler duty, the pureness specifications remaining required simultaneously.
Background technology
Acrylonitrile manufacture process produces HCN.HCN must remove from acrylonitrile in the process, in order to meets final acrylonitrile specification.HCN can be valuable by-product, in order to expect that this process reclaims the HCN purified.In order to make Human body package minimize, system is in position to remove HCN, and reduces the exposure to HCN during equipment operation or maintenance.In certain aspects, the system that manufactures utilizes the equipment that can process HCN with low risk of leakage.Such as, the system utilizing gravity stream contributes to the elimination needs to pump in HCN processes.But, fouling (particularly column plate (tray)) is typically the problem in acrylonitrile equipment.The polymerization of HCN can be the problem in acrylonitrile process.
It is directed to use with head fraction column for removing an important system of HCN in acrylonitrile manufacture process.Head fraction column 30 includes multiple column plate.In one embodiment, head fraction column 30 include 50 (50) and 75 (75) individual between column plate, alternatively individual 55 (55) to 65 (65) between column plate.In an embodiment, head fraction column 30 includes 62 (62) individual column plates, alternatively 60 (60) or 65 (65) column plates.Head fraction column 30 may be configured to receive crude product nitrile feed stream 1 at column plate 28.In an embodiment, column plate 28 the most all can start between the 35th and the 48th column plate from the bottom of head fraction column 30, preferably between 40 to four ten four four ten column plates.Side stream (sidedraw) that head fraction column 30 may be configured to from head fraction column removes effluent 44, side stream and include that bottom from head fraction column 30 starts between the 15th and the 28th column plate in all cases, the water between preferably 18 and 25 column plates and Organic substance.In an alternative embodiment, column plate 28 can be the 42nd or the 38th column plate started from the bottom of head fraction column 12.
In an alternative embodiment, column plate 28 can be the 47th column plate started bottom head fraction column 30, and head fraction column 30 can include 67 column plates.In an embodiment, the first to two ten bottom tray of head fraction column 30 are dried acrylonitrile product.In an embodiment, the 21st to the 42nd column plate started bottom head fraction column 30 removes and purifies HCN.In an embodiment, head fraction column 30 include 40 (40) and 65 (65) individual between column plate.In an embodiment, and feed tray 28 between the 20th and the 30th column plate started from head fraction tower bottom, and can include them.
In some designs, head fraction column includes two the tower sections stacked on top of each other.In this design, bottom section is referred to as drying tower/section, and includes between 15 and 30 column plates, between preferably 18 and 25, between more preferably 18 and 22.In another aspect, head fraction column includes column plate 1 to 20, and wherein column plate 1 is the column plate of bottom.Head tower section is the position that HCN distills at tower top, and it is referred to as head fraction column/section or HCN tower/section, and in an aspect, including the column plate between 30 and 50, between preferably 32 and 48, and the column plate between more preferably 38 and 48.In another aspect, tower includes column plate 21 to 62, and wherein column plate 62 is the highest column plate.These numbers can be different in different head fraction columns.
In order to contribute to reducing fouling, conventional head fraction drying tower operates under reducing pressure (vacuum) operation.This operator scheme reduces fouling sharp, and extends the operating time between HCN or the cleaning of head fraction column.HCN or head fraction column operation under reducing pressure need to distill at a lower temperature.The polymerization rate producing the solid making process device fouling greatly reduces at a lower temperature.But, as compromise, lower temperature distillation needs to provide relatively low condensation temperature.This needs freezing coolant, such as, the ethylene-ethylene glycol-water mixture of cooling, commonly referred to " salt (brine) ".Salt needs the temperature of about 0 DEG C possibly for head fraction column condenser, and needs the temperature of about-10 DEG C at relief condenser.
Utility model content
A kind of process reclaimed for acrylonitrile includes providing to be provided the feed stream including acrylonitrile, HCN and water to head fraction column；In head fraction column, distill this feed stream produce and include that the head fraction column overhead (overhead) of HCN flows and includes the bottom liquid stream of acrylonitrile；From including that water and sideing stream of organic head fraction column remove effluent；Organic streams is provided from effluent separation at least some water and Organic substance；Organic streams is made to return head fraction column；With adjustment from the ratio of the amount of the effluent removed that sides stream of head fraction column with the amount of the organic streams returning head fraction column in lower section of sideing stream, to provide the HCN of 500ppm or less to bottom liquid stream.
A kind of process reclaimed for acrylonitrile includes providing to head fraction column the feed stream including acrylonitrile, HCN and water；In head fraction column, distill this feed stream produce the head fraction column column overhead stream including HCN and the bottom liquid stream including acrylonitrile；From including that water and sideing stream of organic head fraction column remove effluent；From effluent separation at least some water and Organic substance；With Organic substance is divided at least two plumes, and make this stream return to the separate position of at least two on head fraction column.
A kind of process for operating head fraction column includes providing to head fraction column the feed stream including acrylonitrile, HCN and water；This feed stream is distilled to produce head fraction column column overhead stream and this head fraction column overhead is streamed to head fraction column condenser in head fraction column；Sideing stream to remove and include water and organic effluent from head fraction column, and effluent is sent to effluent heat exchanger to provide the effluent of cooling；From effluent separation at least some water and the Organic substance of cooling；Organic streams is made to return head fraction column；With adjustment from the ratio of the amount of the effluent removed that sides stream of head fraction column with the amount of the organic streams returning head fraction column in lower section of sideing stream, with heat load and the ratio of heat load in effluent heat exchanger in the head fraction column condenser of offer about 2.5 or less.
A kind of process reclaimed for acrylonitrile includes providing to head fraction column the feed stream including acrylonitrile, HCN and water；In head fraction column, distill the bottom liquid stream that this feed stream produces the head fraction column column overhead stream including HCN, includes acrylonitrile, and include water and the organic effluent sideed stream from head fraction column；Wherein, in tower, the vapor/liquid mol ratio of the top of sideing stream of tower is of about 0.25 and is of about 0.50 to about 0.65 to the vapor/liquid ratio of the lower section of sideing stream of tower in about 0.55, and tower.
A kind of process reclaimed for acrylonitrile includes providing to head fraction column the feed stream including acrylonitrile, HCN and water；In head fraction column, distill the bottom liquid stream that this feed stream produces the head fraction column column overhead stream including HCN, includes acrylonitrile, and include water and the organic effluent sideed stream from head fraction column；Wherein, in tower, the vapor/liquid mol ratio of the top of sideing stream of tower is of about 0.40 to about 1 with the ratio of the vapor/liquid mol ratio of the lower section of sideing stream of tower in tower.
A kind of head fraction column system includes: head fraction column, it is configured to receive the feed stream including acrylonitrile, HCN and water, and be also configured in head fraction column distill feed stream, include the head fraction column column overhead stream of HCN to produce and include the bottom liquid stream of acrylonitrile；Sideing stream, it is configured to remove water and organic admixture from head fraction column and cooled down water and this admixture organic before entering decanter；This decanter is configured to the water in separated flow and organic streams and organic admixture；Diverter, it is configured to receive organic streams from decanter and organic streams is divided at least two plumes；It is configured to above sideing stream, be sent to one in organic streams at least one reflux pipeline of head fraction column；Be configured in lower section of sideing stream, one in organic streams is sent at least one reflux pipeline of head fraction column.
Technical scheme 1: a kind of head fraction column system, including:
Head fraction column；
Side stream；
Decanter；
Diverter, it receives organic streams from described decanter and this organic streams is divided at least two plumes；
Head fraction column the first organic streams entrance；
Head fraction column the second organic streams entrance；
One in organic streams is sent to above described sideing stream at least one return line of described head fraction column the first organic streams entrance；With
One in organic streams is sent in described lower section of sideing stream at least one return line of described head fraction column the second organic streams entrance.
Technical scheme 2: according to the system described in technical scheme 1, it is characterised in that described head fraction column the first organic streams entrance is 5 to 1 column plate of the top of sideing stream of described head fraction column.
Technical scheme 3: according to the system described in technical scheme 1, it is characterised in that described head fraction column the second organic streams entrance is 1 column plate of the lower section of sideing stream of described head fraction column.
Technical scheme 4: according to the system described in technical scheme 1, it is characterised in that described in side stream and cooled down at least one heat exchanger.
Technical scheme 5: according to the system described in technical scheme 4, it is characterised in that described in side stream and fed by gravity and be transferred into described heat exchanger.
Technical scheme 6: according to the system described in technical scheme 1, it is characterised in that the discharge stream from described decanter returns described head fraction column.
Technical scheme 7: according to the system described in technical scheme 4, it is characterised in that described head fraction column column overhead stream is transferred into head fraction column condenser.
Technical scheme 8: according to the system described in technical scheme 7, it is characterised in that in described head fraction column condenser, heat load is 2.5 or less with the ratio of heat load in the heat exchanger that sides stream.
Technical scheme 9: according to the system described in technical scheme 1, it is characterised in that described head fraction column include described in side stream lower section 15 to 30 column plates.
Technical scheme 10: according to the system described in technical scheme 9, it is characterised in that described head fraction column include described in side stream lower section 18 to 25 column plates.
Technical scheme 11: according to the system described in technical scheme 10, it is characterised in that described head fraction column include described in side stream lower section 18 to 22 column plates.
Technical scheme 12: according to the system described in technical scheme 1, it is characterised in that described head fraction column include described in side stream top 30 to 50 column plates.
Technical scheme 13: according to the system described in technical scheme 12, it is characterised in that described head fraction column include described in side stream top 32 to 48 column plates.
Technical scheme 14: according to the system described in technical scheme 13, it is characterised in that described head fraction column include described in side stream top 38 to 44 column plates.
Accompanying drawing explanation
According to the following drawings, if the above and other aspects, features and advantages of the drying method of this process will become apparent from.
Fig. 1 shows head fraction column system.
Fig. 2 shows the head fraction column system with pump circulation (pump around).
Fig. 3 shows the another aspect of the head fraction column system with pump circulation.
Corresponding reference number represents the counterpart member of the some views running through accompanying drawing.It will be recognized that element in accompanying drawing is in order to simple and clear and illustrate, and be not necessarily drawn to scale.Such as, the big I of some elements in accompanying drawing is exaggerated relative to other elements, to contribute to improving the understanding of various aspect.It addition, do not draw at the common but well-understood element that the aspect of commericially feasible is useful or required, in order to the observation to these various aspects hinders less.
Detailed description of the invention
Hereinafter describe and consider the most in a limiting sense, be only used for describing the General Principle of example embodiment and making.Scope of the present utility model should determine with reference to claim.
A kind of process and equipment include head fraction column.Head fraction column receives crude product nitrile feed stream (it includes acrylonitrile, HCN and water).Distillation in head fraction column provides the head fraction column column overhead stream including Blausure (German) (HCN) at head fraction column top, and the head fraction column bottom liquid including acrylonitrile product at place bottom head fraction column.Column distillation causes both Blausure (German) and water to remove from acrylonitrile.
Head fraction column column overhead stream is sent to head fraction column condenser, here, a part is used coolant to condense.Uncooled steam from head fraction column condenser is sent to head fraction column relief condenser, here, a part is used coolant to condense.This process includes combining from head fraction column condenser and two kinds of condensate liquid stream of head fraction column relief condenser, and those are streamed to head fraction column reflux pump.A part for the liquid stream of this combination is back to the top of head fraction column as backflow, and remainder is used as product or throws aside.
This process is included at the centre portion of head fraction column and removes whole liquid distillates, and this fraction is delivered to effluent cooler and is then sent to decanter.Before, first liquid distillate will go to heat exchanger, here, the colder organic streams from decanter will cool down whole liquid distillate stream.Then whole liquid distillate stream will advance to head fraction column decanter, occur at this to be separated.Aqueous phase from the water side of decanter can go to recovery tower feed manifold.Acrylonitrile from the Organic substance side of decanter returns head fraction column mutually.
In one aspect, this process includes head fraction column provides the feed stream including acrylonitrile, HCN and water.As it is shown in figure 1, enter head fraction column 30 at head fraction column 30 upper curtate that feed stream 34 is at head fraction column feed stream 36.In one aspect, feed stream 36 may correspond to any one in the number of plates 40 to 45 of head fraction column 30, and in another aspect, corresponding to the number of plates 42 of head fraction column 30.Feed stream 34 can include acrylonitrile and the HCN of about 5 to about 13 percentage by weights of about 82 to about 90 percentage by weights.
This process is included in head fraction column 30 distillation feed stream 34, to produce the head fraction column column overhead stream 51 including HCN and the bottom liquid stream 58 including acrylonitrile.This process includes 44 removing effluent 46 from sideing stream of head fraction column 30.In one aspect, 44 are sideed stream at the centre portion of head fraction column 30.In another aspect, 44 any one that may correspond in the number of plates 18 to 23 of head fraction column 30 (it includes 62 column plates) of sideing stream, and in another aspect, corresponding to the number of plates 21 of head fraction column 30.Effluent 46 includes water and Organic substance.
In one aspect, 44 allowing in tower of sideing stream are taken out at the height of effluent 46, effluent 46 includes the acrylonitrile of about 90 to about 95 percentage by weights, and in another aspect, the acrylonitrile of about 92 to about 93 percentage by weights, and the water of about 5 to about 10 percentage by weights, and in another aspect, the water of about 7 to about 8 percentage ratios.
As it is shown in figure 1, this process can include using effluent pump 39 to remove effluent 46 continuously from head fraction column 30.This process includes cooling down effluent 46 to provide the effluent 49 of cooling.Process shown in Fig. 1 includes making effluent 46 through the first heat exchanger 35 and the second heat exchanger 37.This process provides the effluent 49 of cooling, and the effluent 49 of this cooling had about 35 DEG C to about 45 DEG C, and the temperature of the most about 38 DEG C to about 42 DEG C before entering decanter 33.The effluent 49 that decanter 33 provides this cooling improves water and organic separation.
Water and organic material separate in decanter 33.Pump (not shown) removes aqueous phase 42 from decanter 33.Organic streams pump 31 removes organic streams 48 from decanter 33.In decanter 33, one is mainly water (about 93%) mutually, and another phase is acrylonitrile (about 95%).Aqueous phase is pumped to recovery tower feed manifold (not shown) from the water side of decanter 33.Acrylonitrile from the Organic substance side of decanter 33 is pumped back head fraction column 30 mutually.
Decanter discharge stream 47 can be sent to scrubber's (not shown).Organic streams 48 is transferred into the first heat exchanger 35, provides cooling stream this its.Organic streams 48 enters head fraction column 30 at organic streams entrance 54.Organic streams entrance 54 can be at the centre portion of head fraction column 30.In this aspect, organic streams entrance 54 is sideing stream below 44.
In another aspect, this process includes head fraction column column overhead stream 51 is sent to head fraction column condenser 55.Head fraction column column overhead stream 51 uses condenser coolant stream 53 to condense in head fraction column condenser 55.In in this regard, condenser coolant stream 53 is antifreezing agent or chilled water.Condenser coolant stream 53 has the temperature of about-10 DEG C to about+10 DEG C, in another aspect, about-10 DEG C to about+5 DEG C.Vapor/liquid stream 92 is sent to vapour/liquid separator 94.Uncooled steam 58 from vapour/liquid separator 94 is sent to head fraction column relief condenser 90.Uncooled steam 58 condenses in the head fraction column relief condenser 90 cooled down by discharge coolant stream 61.In in this regard, discharge coolant stream 61 can be antifreezing agent or chilled water.Discharge coolant stream 61 has the temperature of about-10 DEG C to about+10 DEG C, in another aspect, about-10 DEG C to about+5 DEG C.Vapor/liquid stream 96 is sent to second liquid/vapour separator 98.
In another aspect, this process includes combining head fraction column condenser condensate 63 and head fraction column relief condenser condensate 65, to form the condensate flow 67 of combination.This process also includes utilizing condensate pump 71 that the condensate flow 67 of combination is sent to the top section of head fraction column 30.This process may be included in a part for the condensate flow 67 extracting combination at outlet port 74 out.The condensate flow 67 of combination can return the top section of head fraction column 30 at head fraction column condensate entrance 76.
As in figure 2 it is shown, and be similar to Fig. 1, this process includes providing head fraction column including the feed stream of acrylonitrile, HCN and water.As in figure 2 it is shown, enter head fraction column 30 at the upper curtate of the head fraction column 30 that feed stream 34 is at head fraction column feed stream 36.In one aspect, feed stream 36 may correspond to any one in the number of plates 40 to 45 of head fraction column 30 (it includes 62 column plates), and in one aspect, corresponding to the number of plates 42 of head fraction column 30.This process is included in head fraction column 30 distillation feed stream 34, to produce the head fraction column column overhead stream 51 including HCN and the bottom liquid stream 58 including acrylonitrile.In in this regard, bottom liquid stream 58 includes the HCN of about 500ppm or less, in another aspect, the HCN of about 0 to about 500ppm, in another aspect, the HCN of about 1 to about 400ppm, in another aspect, the HCN of about 1 to about 250ppm, and in another aspect, the HCN of about 1 to about 100ppm.Bottom liquid stream 58 may also comprise the water of about 0.1 to about 0.5 percentage by weight, in another aspect, the water of about 0.1 to about 0.25 percentage by weight.
Head fraction column column overhead stream 51 includes the acrylonitrile of about 100ppm or less, in another aspect, the acrylonitrile of about 0 to about 100ppm, in another aspect, the acrylonitrile of about 1 to about 90ppm, in another aspect, the acrylonitrile of about 5 to about 50ppm, in another aspect, the acrylonitrile of about 5 to about 25ppm, and in another aspect, the acrylonitrile of about 1 to about 10ppm.Head fraction column column overhead stream 51 can include the water of about 0.25 to about 0.75 percentage by weight, in another aspect, the water of about 0.4 to about 0.6 percentage by weight.
This process includes 44 removing effluent 46 from sideing stream of head fraction column 30.In one aspect, 44 are sideed stream at the centre portion of head fraction column 30.In another aspect, 44 any one that may correspond in the number of plates 18 to 23 of head fraction column 30 of sideing stream, and in one aspect, corresponding to the number of plates 21 of head fraction column 30.Effluent 46 includes water and Organic substance.
In an aspect, and different from the process of Fig. 1, the process shown in Fig. 2 includes effluent 46 is sent to heat exchanger 38.In in this regard, effluent 46 may utilize gravity charging and flow to heat exchanger 38.This process provided the effluent 49 of the cooling of the temperature with about 35 DEG C to about 45 DEG C and the most about 38 DEG C to about 42 DEG C before entering decanter 33.In the aspect of the process shown in Fig. 2, this process need not pump and effluent 46 be sent to heat exchanger 38, and only needed single heat exchanger before entering in decanter 33.
In another aspect, water and organic material separate in decanter 33.Pump (not shown) removes aqueous phase 42 from decanter 33.Organic streams pump 31 removes organic streams 48 from decanter 33.Different from Fig. 1, the process shown in Fig. 2 includes organic streams 48 is sent to diverter 71.Organic streams 48 is divided into the first organic streams 73 and the second organic streams 75 by diverter.In in this regard, diverter 71 provides about 40 to about 60 weight % of organic streams 48 to the first organic streams 73 or the second organic streams 75.
In another aspect, this process includes making the first organic streams 73 and the second organic streams 75 return head fraction column 30 in two separate positions of head fraction column 30.In in this regard, this process includes making the first organic streams 73 return head fraction column the first organic streams entrance 77, and makes the second organic streams 75 return head fraction column the second organic streams entrance 79.In one aspect, this process includes making the first organic streams 73 return the first organic streams entrance 77, what it was head fraction column 30 side stream about 5 to about 1 column plates above 44, in another aspect, about 4 to about 1 column plate, in another aspect, about 3 to about 1 column plates, in another aspect, about 2 to about 1 column plates, and in another aspect, about 1 column plate sideed stream above 44 of head fraction column 30.In another aspect, this process includes making the second organic streams 75 return the second organic streams entrance 79, what it was head fraction column 30 side stream about 5 to about 1 column plate below 44, about 4 to about 1 column plate, in another aspect, about 3 to about 1 column plate, in another aspect, about 2 to about 1 column plate, and in another aspect, about 1 column plate sideed stream below 44 of head fraction column 30.
In another aspect and different from Fig. 1, the process shown in Fig. 2 includes decanter discharge stream 47 is sent to head fraction column 30.In in this regard, decanter discharge stream 47 can enter head fraction column 30 at decanter discharge stream entrance 81.Decanter discharge stream entrance 81 may correspond to the position on head fraction column with the 44 identical column plates that side stream.Decanter discharge stream 47 can liquid from side stream 44 remove time be used as balanced line.
Being compared as follows of heat load between the process of Fig. 1 and Fig. 2.
The comparison of the process of Fig. 1 and Fig. 2 reduces about 13% in the case of showing the shunting return that the condenser duty of head fraction column is shown in fig. 2.This change of heat load changes into the saving of refrigeration.This change of heat load is substantially transferred to effluent heat exchanger 38, and effluent heat exchanger 38 uses cooling water, and cooling water is more cheap public things.Although the thermal balance around head fraction column changes significantly due to processing equipment and operation change, but the overall net change of cooling between Fig. 1 and Fig. 2 and reboiler duty is less, it is expected to be 0.62% and 0.43%.In in this regard, effluent heat exchanger 38 has the heat load of 3165kw or less, and in another aspect, about 1410 arrive about 2350kw, and in another aspect, about 2350 arrive about 3165kw (acrylonitrile yield based on 260-350kta).In another aspect, the ratio of the heat load in head fraction column condenser 55 and the heat load in effluent heat exchanger 38 is of about 4.7 or less, in another aspect, about 2.5 or less, in another aspect, about 2 to about 3, and in another aspect, about 2.5 to about 4.7.
In one aspect, the process shown in Fig. 2 provides removing of a heat exchanger and pump, and the reduction that refrigeration communal facility requires.The practical example of this benefit can manifest during fouled condition.When overhead tower starts fouling, the operation of tower tends to that needing more and more refluxes and maintains identical pureness specifications, until final tower must shut off to be cleaned.Owing to the circulation of the pump of column plate 22 to be to increase the source of backflow, therefore which results in the relatively low condenser duty relevant to the fouled condition in head fraction column.
In another aspect, head fraction column is operated under this process is included in certain vapor/liquid mol ratio.In in this regard, the vapor/liquid mol ratio above 44 of sideing stream in head fraction column 30 is of about 0.25 to about 0.55, in another aspect, about 0.26 to about 0.51, in another aspect, 0.26 to about 0.48, in another aspect, about 0.45 to about 0.55, in another aspect, about 0.46 to about 0.51, and in another aspect, about 0.49 to about 0.51.In one aspect, the vapor/liquid mol ratio of the top of sideing stream of the process returned including shunting is of about 0.25 to about 0.50, and in another aspect, about 0.26 to about 0.48.In another aspect, the vapor/liquid mol ratio including the top of sideing stream of the process of single return is of about 0.49 to about 0.51.
The vapor/liquid mol ratio below 44 of sideing stream in head fraction column 30 is of about 0.4 to about 1, in another aspect, about 0.5 to about 0.65, in another aspect, about 0.55 to about 0.65, in another aspect, about 0.54 to 0.61, in another aspect, about 0.56 to about 0.62, and in another aspect, about 0.58 to about 0.61.On the one hand, the vapor/liquid mol ratio of the lower section of sideing stream of the process returned including shunting is of about 0.5 to about 0.65, and in another aspect, about 0.54 to about 0.61.In another aspect, the vapor/liquid mol ratio including the lower section of sideing stream of the process of single return is of about 0.58 to about 0.61.
In another aspect, head fraction column is operated under this process is included in certain vapor/liquid mol ratio.In in this regard, the ratio of the vapor/liquid mol ratio below 44 of sideing stream in the vapor/liquid mol ratio sideed stream in head fraction column 30 above 44 and head fraction column 30 is of about 0.4 to about 0.9, in another aspect, about 0.44 to about 0.88, in another aspect, about 0.75 to about 0.90, in another aspect, about 0.77 to about 0.82, and in another aspect, about 0.82 to about 0.87.In another aspect, during including that shunting returns, the ratio of the vapor/liquid mol ratio below 44 of sideing stream in the vapor/liquid mol ratio sideed stream in head fraction column 30 above 44 and head fraction column 30 is of about 0.4 to about 0.85, and in another aspect, about 0.44 to about 0.83.In another aspect, during including single return, the ratio of the vapor/liquid mol ratio below 44 of sideing stream in the vapor/liquid mol ratio sideed stream in head fraction column 30 above 44 and head fraction column 30 is of about 0.8 to about 0.9, and in another aspect, about 0.81 to about 0.83.
The vapor/liquid ratio above 44 that sides stream in head fraction column 30 can calculate as follows:
Flow velocity in head fraction column column overhead stream 51/(flow velocity in feed stream 34)+(flow velocity of the combined condensates stream 67 at head fraction column entrance 76)
The vapor/liquid ratio below 44 that sides stream in head fraction column 30 can calculate as follows:
The flow velocity of flow velocity/the second organic streams 75 in head fraction column column overhead stream 51.
Fig. 3 is similar to Fig. 1, and simply Fig. 3 includes the heat exchanger 99 added.
Although this utility model disclosed herein describes by means of specific embodiment, example and application thereof, but those skilled in the art can various modifications may be made and modification to it, without deviating from the scope of the present utility model illustrated in claim.
Claims (14)
1. a head fraction column system, including:
Head fraction column；
Side stream；
Decanter；
Diverter, it receives organic streams from described decanter and this organic streams is divided at least two plumes；
Head fraction column the first organic streams entrance；
Head fraction column the second organic streams entrance；
One in organic streams is sent to above described sideing stream at least one return line of described head fraction column the first organic streams entrance；With
One in organic streams is sent in described lower section of sideing stream at least one return line of described head fraction column the second organic streams entrance.
System the most according to claim 1, it is characterised in that described head fraction column the first organic streams entrance is 5 to 1 column plate of the top of sideing stream of described head fraction column.
System the most according to claim 1, it is characterised in that described head fraction column the second organic streams entrance is 1 column plate of the lower section of sideing stream of described head fraction column.
System the most according to claim 1, it is characterised in that described in side stream and cooled down at least one heat exchanger.
System the most according to claim 4, it is characterised in that described in side stream and fed by gravity and be transferred into described heat exchanger.
System the most according to claim 1, it is characterised in that the discharge stream from described decanter returns described head fraction column.
System the most according to claim 4, it is characterised in that described head fraction column column overhead stream is transferred into head fraction column condenser.
System the most according to claim 7, it is characterised in that in described head fraction column condenser, heat load is 2.5 or less with the ratio of heat load in the heat exchanger that sides stream.
System the most according to claim 1, it is characterised in that described head fraction column include described in side stream lower section 15 to 30 column plates.
System the most according to claim 9, it is characterised in that described head fraction column include described in side stream lower section 18 to 25 column plates.
11. systems according to claim 10, it is characterised in that described head fraction column include described in side stream lower section 18 to 22 column plates.
12. systems according to claim 1, it is characterised in that described head fraction column include described in side stream top 30 to 50 column plates.
13. systems according to claim 12, it is characterised in that described head fraction column include described in side stream top 32 to 48 column plates.
14. systems according to claim 13, it is characterised in that described head fraction column include described in side stream top 38 to 44 column plates.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520909226.3U CN205759801U (en) | 2015-11-16 | 2015-11-16 | Head fraction column system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520909226.3U CN205759801U (en) | 2015-11-16 | 2015-11-16 | Head fraction column system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN205759801U true CN205759801U (en) | 2016-12-07 |
Family
ID=57412933
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201520909226.3U Active CN205759801U (en) | 2015-11-16 | 2015-11-16 | Head fraction column system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN205759801U (en) |
-
2015
- 2015-11-16 CN CN201520909226.3U patent/CN205759801U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| RU2617692C2 (en) | Seletive extraction of olefins | |
| US10315971B2 (en) | Process for recovering heat from a hydrocarbon separation | |
| EP3983104B1 (en) | Process for distilling a crude composition in a rectification plant including an indirect heat pump | |
| CN106458792B (en) | Absorption/distillation in a single column design | |
| RU2500450C2 (en) | Perfected heat pump for high-purity bottom product | |
| US20110041550A1 (en) | Process and apparatus for the separation of light-boiling components from hydrocarbon mixtures | |
| JP4983041B2 (en) | Caprolactam purification method | |
| CN205759801U (en) | Head fraction column system | |
| RU2662542C2 (en) | Fractionation system having rectifying and stripping columns in a single vessel with a uniform diameter | |
| TWI639461B (en) | Heads column overhead system | |
| CN106699599A (en) | Heads column pump circulation | |
| US4484984A (en) | Distillation with condensation process | |
| RU2811786C2 (en) | Method for distillation of crude composition in rectification plant including indirect heat pump | |
| TWI834895B (en) | Process for distilling a crude composition in a rectification plant including an indirect heat pump and a rectification plant | |
| AU2016296356B2 (en) | Method for purifying a gas rich in hydrocarbons | |
| US20120228116A1 (en) | Vacuum Evaporator / Distillation System | |
| JP2012529623A5 (en) | ||
| CN106045822A (en) | Energy-saving phenol refining device with high product segmentation degree, and phenol refining method | |
| JPH04250801A (en) | Method and apparatus for distillation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |