Abstract:
The invention relates to a method and apparatus to recover and purify methanol from gases produced in the digester during the kraft pulping process. The gas is typically recovered as a foul gas (called stripper off gas or SOG) comprising methanol, water and various other contaminants. The gas is then treated with successive decanting and distillation steps to remove impurities, thereby producing highly purified methanol.

Description:
FIELD OF THE INVENTION 
       [0001]    This invention relates to a method and apparatus to recover purified methanol stripped from a foul gas stream. 
       BACKGROUND OF THE INVENTION 
       [0002]    Methanol is formed as a by-product of the kraft pulping process, when the hydroxyl on reacts with a lignin methoxyl group: 
         [0000]      lignin.OCH 3 +OH − →CH 3 OH lignin.O − 
 
         [0003]    Depending on the mill configuration, up to 90% of the methanol generated in the digester can be captured in the foul condensate from the digester and evaporator areas. The foul condensate is typically treated in a steam stripping system, where up to 95% of the methanol can be removed from the foul condensate and captured in the overhead vapours from the stripping process. The concentrated gas stream is often referred to as stripper off gas (SOG). 
         [0004]    The SOG is then usually disposed of through thermal oxidation in a lime kiln, power boiler, recovery boiler, or dedicated incinerator. The SOG typically consists of about 40 to 70 wt % methanol, 5 to 10 wt % non-condensable materials, including sulphur compounds, and the balance water vapour. 
         [0005]    Waste SOG can be burned as a replacement for fossil fuels. However, the value of SOG as a fuel depends on the amount of water vapour that it contains. Natural gas provides 50.5 MJ/kg (37.2 MJ/m 3 ) heat of combustion, pure methanol provides 22.7 MJ/kg, and SOG containing 70 wt % methanol provides the equivalent of about 21.9 MJ/kg. The SOG provides less heat because the entrained water vapour must first be heated up to combustion temperature. 
         [0006]    Chlorine dioxide is used in the pulp bleaching process; grade AA methanol (99.85 wt %) is used to manufacture ClO 2 . In a well-run mill, a methanol purification system would preferably be able to produce sufficient amounts of purified methanol for the demands of the ClO 2  process, as well as some purified methanol for external sale. If a substantial portion of the methanol in the SOG can be recovered and purified to an industrial grade AA product, the methanol produced in a typical kraft pulping process could be worth as much as four and a half times more as a commodity than as a fuel. 
         [0007]    There are numerous methanol purification systems in operation. Most such systems use some form of distillation to separate methanol from other compounds. See for example, U.S. Pat. No. 5,718,810 to Robbins and U.S. Pat. No. 6,217,711 to Ryham et al. Canadian Patent No. 1,0888,957 to Suokas et al., uses a combination of distillation steps and acid or alkaline oxidating treatments to separate the various fractions. Distillation separates the components of a solution by partial vapourization of the mixture and separate recovery of vapour and residual liquid. The more volatile constituents of the original mixture are obtained in increased concentration in the vapour, while less volatile components remain in greater concentration in the liquid residue. Distillation columns may be designed using trays, structured packing, or random dumped packing. Due to restricted access, for small columns below about 750 mm diameter, random dumped packing is preferred. 
         [0008]    However, methanol recovered from a kraft pulping process has several unique characteristics that inhibit separation by distillation. 
         [0009]    Typically, significant quantities of dimethyl disulphide are present in the crude methanol produced during the kraft pulping process. The presence of an azeotrope between methanol and dimethyl disulphide requires that the methanol content in the SOG be no higher than approximately 40 wt % to ensure separation. Control of the foul condensate steam stripping system, in terms of both the quantity and quality of SOG produced, can reduce the impact of azeotropes of dimethyl disulphide. Many existing stripping systems include a reflux condenser integrated with the multiple effect evaporators; see for example U.S. Pat. No. 4,137,134 to Suominen et al., U.S. Pat. No. 3,807,479 to Brannland et al., and U.S. Pat. No. 5,830,314 to Mattsson. Unfortunately, in this arrangement, control of the stripping system may be compromised because any fluctuations in evaporator operation will ripple through the stripping system, unpredictably affecting SOG quantity and quality. 
         [0010]    Further, contaminants including ionizable sulphur compounds such as hydrogen sulphide and methyl mercaptan are produced during the pulping process. These compounds can dissociate under certain conditions, making them all but impossible to remove from SOG by simple distillation. As can be seen in  FIG. 1 , hydrogen sulphide (H 2 S) begins to dissociate at a pH above about 6, while methyl mercaptan (MM) begins to dissociate at a pH above about 9. In their dissociated form, these compounds do not exert a vapour pressure and therefore can not be removed by distillation. Controlling the pH of the liquid phase in the distillation column is therefore an effective way to remove these compounds in a distillation process. 
         [0011]    As condensed SOG typically has a pH of about 9 to 10, an acid, such as sulphuric acid, may be metered to the appropriate distillation column to lower the pH in the system. However, the acid cannot simply be added to the liquid feed to the column as it will react with any ammonia present in the system, producing ammonium sulphate. This is known as fouling the column and is to be avoided. U.S. Pat. No. 5,989,394 to Johansson et al. describes a process in which an acidifier is introduced to a stripping column above the admission point of the liquid being purified, or alternatively is added to the liquid feed directly. However, Johansson is concerned with producing a relatively purified condensate stream, rather than removal and high level purification of methanol from the liquid feed stream and does not seem to be concerned with fouling the column. 
         [0012]    It is therefore an object of the invention to provide a method and apparatus to recover and purify methanol stripped from a foul gas stream that overcomes the foregoing deficiencies. 
         [0013]    In particular, it is an object of the invention to provide a method and apparatus to recover and purify methanol to a high degree, allowing methanol to be used within a kraft pulping process and to allow excess methanol to be sold, rather than destroyed. 
         [0014]    These and other objects of the invention will be appreciated by reference to the summary of the invention and to the detailed description of the preferred embodiment that follow. 
       SUMMARY OF THE INVENTION 
       [0015]    The invention relates to a method and apparatus to recover and purify methanol from gases produced in the digester during the kraft pulping process. The gas is typically recovered as a foul gas (called stripper off gas or SOG) comprising methanol, water and various other contaminants. 
         [0016]    Stripper off gas is stripped from the digester and evaporator areas of the pulping process; the SOG then passes, at a controllable flow rate to a dedicated condensing means, where volatile components are boiled off and vented to an incineration system, while the condensate drains to a topping red oils removal means, such as a decanter. Heavy contaminants that are immiscible in the solution are decanted and recovered separately. The underflow is moved to a first distillation means, such as a topping column and heated. Acid is added to the mid-point of the topping column to lower the pH of the solution without allowing the acid to react with ammonia in the feed. Volatile components are returned to the condensing means, while the underflow moves to a surge tank, which may be used to stabilize the flow and concentration of the feed to the rectification section. 
         [0017]    The rectification section may comprise one or two columns. The feed is introduced near the top of the bottoms section of the column, and moves down through the packing in the column, countercurrent to the stripping steam flow. Vaporized methanol moves up through the top section of the column, and any impurities are removed as the overhead vapor flow. Water and other less volatile components form the underflow, while fusel oils are drawn off in a side stream. Purified methanol is drawn off and passed to a methanol cooler for condensation and storage. The methanol is at least 99.85 wt % pure. 
         [0018]    Alternatively, the bottoms section and the top section may each be a separate column. The feed is introduced near the top of the bottoms column, and moves down through the packing in the column, countercurrent to the stripping steam flow. Vaporized methanol is removed as the overhead vapor flow. Water and other less volatile components form the underflow, while fusel oils are drawn off in a side stream. The methanol vapor is passed to the rectification top column, where it is distilled again. Condensate from the rectification top column is returned to the rectification bottoms column, while vapors are collected and condensed before being vented to the incineration system. Purified methanol is drawn off and passed to a methanol cooler for condensation and storage. The methanol is at least 99.85 wt % pure. 
         [0019]    In one aspect, the invention comprises a method to recover and purify methanol from a stripped off gas stream, comprising the steps of: obtaining, at a controlled rate, a foul gas feed comprising no more than approximately 40 wt % methanol; condensing the foul gas feed; removing immiscible contaminants from the condensed foul gas feed; heating the condensed foul gas feed in the presence of an acid to evaporate volatile components, leaving a contaminated methanol feed, the acid being supplied at an entry point below an input point of the condensed foul gas feed; refining the contaminated methanol feed by heating to evaporate methanol from the contaminated methanol feed; and further refining the evaporated methanol by heating to evaporate remaining volatile components and to produce purified methanol and impure condensate. The purified methanol may be cooled and collected for storage. The condensate may be recycled to the step of refining the contaminated methanol feed. 
         [0020]    In a further aspect, excess foul gas may be diverted to a disposal system prior to the condensing step. 
         [0021]    In yet a further aspect, fusel oils may be stripped from the contaminated methanol feed during the refining step. 
         [0022]    In further aspect, the invention may comprise the further step of storing the contaminated methanol feed prior to refining the contaminated methanol feed. 
         [0023]    In a further aspect, the immiscible contaminants may be removed by decanting the immiscible contaminants. 
         [0024]    In another aspect, the invention comprises an apparatus to recover and purify methanol from a stripped off gas stream, comprising: condensing means to receive and condense a controlled amount of stripped off gas comprising no more than approximately 40 wt % methanol; decanting means to remove immiscible contaminants from the condensed gas; first distillation means comprising upper and lower sections, to receive the condensed gas in the upper section, and to heat the condensed gas in the presence of acid received in the lower section, to evaporate volatile components, leaving contaminated methanol; a first refining section to evaporate methanol from the contaminated methanol; and a second refining section to evaporate and condense impurities from the evaporated methanol, producing purified methanol. Means may also be provided to capture and condense the purified methanol for storage 
         [0025]    In a further aspect, the apparatus of the invention may comprise storage means to store the contaminated methanol prior to entering the first refining section. 
         [0026]    In a further aspect, the apparatus of the invention may comprise means to remove fusel oils from the contaminated methanol. 
         [0027]    In another aspect, the first distillation means of the apparatus of the invention may comprise a topping column. The topping column may further comprise a reboiler to recycle part of the contaminated methanol. 
         [0028]    In yet another aspect, the first and second refining sections of the apparatus of the invention may comprise a second distillation means. The second distillation means may comprise a rectification column, or first and second rectification columns. 
         [0029]    In a further aspect, the apparatus of the invention may comprise means to divert excess gas to a disposal system prior to entering the condensing means. 
         [0030]    The foregoing was intended as a broad summary only and of only some of the aspects of the invention. It was not intended to define the limits or requirements of the invention. Other aspects of the invention will be appreciated by reference to the detailed description of the preferred embodiment and to the claims. 
         [0031]    The inventors thank Alberta-Pacific Forest Industries Inc. for its continued interest in this work and for its assistance in testing the system. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0032]    The preferred embodiment of the invention will be described by reference to the drawings in which: 
           [0033]      FIG. 1  is a graph showing the dissociation fractions for hydrogen sulphide and methyl mercaptan at various pH levels; 
           [0034]      FIG. 2  is a schematic of the topping section of the invention; 
           [0035]      FIG. 3  is a schematic of the rectification section of the invention; and 
           [0036]      FIG. 4  is a schematic of an alternative layout of the rectification section of the invention. 
       
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
       [0037]    Stripper off gas (SOG), typically containing about 40 to 70 wt % methanol, is produced in an existing foul condensate steam stripping column. The SOG is directed to a methanol purification system  10 , being diverted from a kiln, boiler, incinerator or other incineration system  12 , as shown in  FIG. 2 . 
         [0038]    Vapour  14  from the existing stripping column is introduced to a dedicated reflux condenser  16 ; this vessel may be of any suitable type, such as a falling film type shell and tube evaporator effect. The heat from the stripping system may be utilized in the evaporator system, but use of a dedicated vessel allows sufficient control over the system to ensure stable qualities and quantities of SOG are produced under all evaporator operating conditions. Pressure is maintained by throttling the flash vapour from the system. 
         [0039]    SOG is introduced to the methanol purification system  10  at a controlled flow rate, with any excess gas being diverted to the incineration system  12 . This helps to maintain the methanol entering the purification system  10  at an optimal content of approximately 40 wt % or less. 
         [0040]    The topping column system  18  strips out low boilers and non-condensables from the SOG, including malodorous sulphur compounds, ammonia, and some ethers, ketones and aldehydes. When SOG is introduced to the topping reflux condenser  20 , the low boilers and non-condensables are vented  22  back to the incineration system  12  while the condensate is drained  24  to the topping red oils decanter  26 . 
         [0041]    Topping red oils pump  28  moves the decanted red oils to a turpentine recovery system (not shown), if available. The underflow  32  from the decanter  26  is moved to the topping column  34  by any suitable means, such as topping reflux pump  36 . A topping reboiler  38  may be used to provide heat to the topping column  34 , evaporating the volatile contaminants in a stream  42 , which can be returned to the topping reflux condenser  20  or otherwise disposed of. 
         [0042]    Sulphuric acid may be added to topping column  34  by any suitable means, such as feed pump  44 . Preferably the acid is added about the mid-point of the column, or at any rate at an entry point  46  below the input point  48  of the condensed underflow feed from the topping reflux pump  36 . The separation between the feed input point  48  and the acid entry point  46  allows any highly volatile ammonia present in the underflow feed to be stripped out in the upper section of the topping column  34  before it has a chance to react with the acid, thereby avoiding the formation of ammonium sulphate precipitates. The acid reduces the pH in the lower section of the topping column  34 , releasing dissociated hydrogen sulphide and methyl mercaptan, which will rise to the upper section of topping column  34 , where it can be removed as part of volatile contaminant stream  42 . 
         [0043]    The underflow  50  from the topping column  34  flows to the surge tank  52 , with some being recycled to topping reboiler  38 . As the flow and concentration of SOG can vary significantly depending on the operation of the existing stripping system, the surge tank can smooth out the flow and concentration of the feed to the methanol rectification column system  54 . 
         [0044]    The feed enters rectification system  54  from surge tank  52 , such as by rectification feed pump  56 . The rectification column system  54  comprises two sections, namely a bottoms stripping section  97  and a top rectification section  99 , as shown in  FIG. 3 . The feed is introduced to the stripping section  97  of column  55  and flows down through the packing, countercurrent to the stripping steam  57 , which may be supplied by a rectification reboiler  59 . The volatile component, including methanol, moves upward to the top rectification section  99 , while the less volatile component, which is mainly water along with other high boilers, is removed as the underflow  63 . 
         [0045]    The feed may also comprise intermediate boilers, such as some higher alcohols (primarily ethanol), higher ketones, etc. These components, often referred to as fusel oils, are drawn off from the bottoms column  55 , preferably at a point  65  located below the feed introduction point  67 . The fusel oils can be recovered separately, or may be combined with the underflow  63  from the column  55 , passing to effluent treatment through rectification bottoms pump  69 . 
         [0046]    The overhead vapour flow  61 , comprising methanol and other volatiles, from upper rectification section  99  is condensed in a rectification reflux condenser  71 , located above column  55 . Any low boilers and non-condensables  73  may be vented to the incineration system  12 . 
         [0047]    The remaining product, which is approximately 99.85 wt % methanol, is drawn off in a stream  75 , preferably located slightly below the top of the packing in top rectification section  99 , and moved to a methanol cooler  77  by suitable means such as by methanol pump  79 , where it can be moved to storage. The methanol product is preferably drawn off in sufficient quantities to maintain the methanol profile in the column. 
         [0048]    Alternatively, the two sections of rectification column system  54  may be supplied in two separate columns, the rectification bottoms column  60  and the rectification top column  62 , as shown in  FIG. 4 . The feed is introduced  64  to the stripping section of the bottoms column  60  and flows down through the packing, countercurrent to the stripping steam  66 , which may be supplied by a rectification reboiler  68 . The volatile component, including methanol, is removed into the overhead vapour flow  70 , while the less volatile component, which is mainly water along with other high boilers, is removed as the underflow  72 . 
         [0049]    In this embodiment, the fusel oils are drawn off from the bottoms column  60 , preferably at a point  74  located below the feed introduction point  64 . Again, the fusel oils can be recovered separately, or may be combined with the underflow  72  from the column  60 , passing to effluent treatment through rectification bottoms pump  76 . 
         [0050]    The overhead vapour flow  70  from rectification bottoms column  60  is directed to the lower section of the rectification top column  62 . Any condensate  80  collected in the bottom of the top column  62  may be returned by an intermediate rectification pump  82  to introduction point  84  of the bottoms column  60 . Vapour  86  from the top column  62  is condensed in a rectification reflux condenser  88 , located above top column  62 . Any low boilers and non-condensables  78  may be vented to the incineration system  12 . 
         [0051]    The remaining product, which is approximately 99.85 wt % methanol, is drawn off in a stream  90 , preferably located slightly below the top of the packing in top column  62 . Again, the methanol product is preferably drawn off in sufficient quantities to maintain the methanol profile in the column and moved to the methanol cooler  94  by suitable means such as by methanol pump  92 , where it can be moved to storage. 
         [0052]    It will be appreciated by those skilled in the art that other variations to the preferred embodiment described herein may be practised without departing from the scope of the invention, such scope being properly defined by the following claims.