Patent Application
20110095233
This invention relates to a method for the production of synthesis gas
“Synthesis Gas”, or “Syngas”, is a mixture of carbon monoxide (CO) and hydrogen (H2), typically when produced in the molar ratio CO:H2 of 1:3 or 1:1.
Currently Synthesis Gas is made by one of two processes, either from coal by gasification with oxygen, usually from air, and water, or from methane by reforming with oxygen (known as thermal reforming or partial oxidative reforming) or water (known as steam reforming).
The chemical reactions associated with the formation of Synthesis Gas from carbon, usually from coal, are as follows:
C+H2O→CO+H2(gasification)
The CO:H2 ratio produced in this way may not be correct for use in downstream synthesis processes. The water gas shift reaction as described below is thus used to adjust the CO:H2 ratio.
CO+H2O→CO2+H2
This adjustment results in the emission of CO2 or water depending on the required adjustment.
Similarly for methane, Syngas can be produced by the following reaction:
CH4+H2O→CO+3H2(reforming)
The CO:H2 ratio produced in this way may not be correct for use in downstream synthesis processes. The water gas shift reaction as described above is used to adjust the CO:H2 ratio. This adjustment also results in the emission of CO2 or water depending on the required adjustment.
There are many reactors which are commercially used to produce Synthesis Gas. These include reactors based on the Lurgi process, the Winkler process and the Wellman process.
The Syngas produced is used, in turn, to produce a wide range of carbon based chemicals. For example, methanol and other hydrocarbon products are made from Synthesis Gas via various processes. Ammonia is another product synthesised from Synthesis Gas in reaction with the nitrogen in air.
The Syngas production processes are endothermic and, as a consequence, a considerable amount of energy is required to run these processes and, to meet these requirements, there are significant carbon dioxide emissions. It is noted that carbon dioxide is a major greenhouse gas, and hence its emission into the atmosphere is not environmentally friendly.
It is an object of this invention to provide a method of producing Synthesis Gas which will at least partially alleviate some of the abovementioned problems.
In accordance with this invention there is provided a method of producing Synthesis Gas which includes combining the product of a coal gasification reaction with the product of a methane reforming reaction.
A further feature of the invention provides ratio of coal fed to the coal gasification reaction to natural gas fed to the methane reforming reaction to be varied to produce Synthesis Gas of predetermined composition.
According to one aspect of the invention there is provided for the coal gasification reaction to occur separately from the methane reforming reaction and for the products of the separate reactions to be combined.
Further according to this aspect of the invention there is provided for the product of at least the gasification reaction to have undesirable components removed therefrom prior to combining with the product of the methane reforming reaction; alternatively or in addition for undesirable components to be removed from the Synthesis Gas after production thereof.
According to a second aspect of the invention there is provided for the coal gasification reaction to occur in the same vessel as the methane reforming reaction.
Further according to this aspect of the invention there is provided for undesirable components to be removed from the Synthesis Gas after production thereof.
The invention also provides a Synthesis Gas production unit which includes a coal feed and a natural gas feed and wherein the unit subjects the coal feed to a gasification reaction and the natural gas to a methane reforming reaction.
A further feature of the invention provides for gasification reaction and reforming reaction to take place simultaneously.
According to one aspect of the invention there is provided for the gasification reaction to take place in a separate vessel to the reforming reaction.
Further according to this aspect of the invention there is provided for the unit to include means for combining the products of the gasification reaction and reforming reaction; and for the unit to include means for removing undesirable components from the product of the gasification reaction.
According to a second aspect of the invention there is provided for the gasification reaction to take place in the same vessel as the reforming reaction.
Further according to this aspect of the invention there is provided for the unit to include means for removing undesirable components from the Synthesis Gas produced.
While coal gasification processes have been widely used for the production of Synthesis Gas because of the cost benefits of using coal as the major starting material, these processes are, by their very nature, inefficient in energy consumption and produce large carbon dioxide emissions. According to the present invention the products of the methane reforming process is combined with that of the carbon gasification reaction. It has been found that combining the products of the methane reforming reaction and the carbon gasification reaction facilitates the more efficient use of coal and methane resources while reducing the environmental impact per ton of product produced.
The combination of the products of methane and coal reactions has been demonstrated to result in a synergistic effect, even with minor additions of methane to the process. This benefit has been found to result from the preferred heat of combustion of the methane combustion together with the capacity to adjust the carbon:hydrogen ratio. The benefits include:
These benefits result primarily from a reduction in carbon dioxide emissions and it is this aspect in particular that is a quite unexpected result of combining the products of the gasification and reforming reactions.
Coal gasification operates in a temperature range of between 500 and 1200° C. and from atmospheric to 70 bars for a variety of commercial implementations. Any of these would be suitable for the application of separate gasification implementations. The gasification process can make use of pure oxygen or an enriched or standard air feed.
Standard methane reforming technologies operate in the temperature range between 700 to 1100° C. and make use of either oxygen (partial oxidation reformers) or steam and oxygen (steam reformers).
The ratio of coal to natural gas used would be varied as required to produce Synthesis Gas of predetermined composition. This greatly assists in economising downstream processing of the Synthesis Gas as it permits the Synthesis Gas to be produced with a desired composition. The temperature of the process can be adjusted to alter the hydrogen, carbon monoxide ratio by means of the water gas shift reaction.
The reactions below do not include the pyrolysis and drying reaction that would take place in the unit.
C+½O2→CO
C+O2→CO2
H2+O2→H2O
These reactions are exothermic and produce the energy required by the endothermic reduction, pyrolysis and cracking reactions.
C+CO2→2CO
C+H2O→CO+H2
Other reactions know to take place in the coal gasifier include:
CO+H2OCO2+H2
C+2H2→CH4
CO+3H2→CH4+H2O
3C+2H2O→CH4+2CO
4CnHm→mCH4+(4n−m)C
2CnHm+(4n−m)H2→2nCH4
CnHm+(2n−m/2)H2→nCH4
Combustion of Methane to provide the required process energy:
CH4+O2→CO+2H2O
CH4+2O2→CO2+2H2O
CH4+O2→CO+2H2
CH4+H2O→CO+3H2
In addition, the water gas shift reaction described above is known to occur in the methane reformers.
The net effect of these reactions is exothermic thus obviating the need to add energy to the process. This results in a significant energy saving over the known individual processes.
The reforming and gasification reactions can be performed either in separate vessels or in a single vessel. While there are scale economic savings to be achieved in the inclusion of these reactions into a single vessel, there are process costs. The product stream from coal gasification is generally far richer in sulphide products and other undesirable components than the methane reformer product. It is usually necessary to remove these components prior to any further processing of the Synthesis Gas to avoid the poisoning of the downstream catalyst beds. Due to the differences in the gasification and product streams, there are advantages to both the merging of the processes and the separation. Where the gas purification technology is more suited to concentrated toxin removal, the separation of coal gasification and methane reforming and the separate cleaning of these streams prior to merging may be desirable. A simple flow diagram of such a process is shown in
It will be understood that the reforming reaction and gasification reaction could take place simultaneously or at different times to each other.
Alternatively, where a gas purification technology is selected that would work preferentially with a lower toxin composition, the integration of the reformer and gasifier reactions would lower the toxins to the point where the technology can be applied, as shown in the flow diagram in
Both of these process combinations would permit the production of any desired carbon monoxide ratio while making the optimal use of the gas purification technology.
A third option, which requires the development of appropriate technology, permits the gasification of the coal and the reforming of the methane in the same vessel. A simple flow diagram of this process is given in
The above examples illustrate a further aspect of the invention, namely a unit for the production of Synthesis Gas. The unit is characterised in that it includes a coal feed and a natural gas feed and in that it subjects the coal feed to a gasification reaction and the natural gas to a methane reforming reaction. These reactions can take place in separate vessels in the unit, as illustrated with reference to
Where the reactions occur in separate vessels the unit will include means for combining the products of the reactions. It will also include means for removing undesirable components from either or both of the product streams. The unit will furthermore include means for varying the ratio of the coal feed to natural gas feed to enable Synthesis Gas of predetermined composition to be produced. This will enable the Synthesis Gas composition to be tailored to suit downstream processes.
The downstream processes in which the Synthesis Gas can be used are many. They include the production of hydrocarbons, such as methanol, and the production of nitrogen-hydrogen complexes such as ammonia. It has been found that integrating downstream processes to produce hydrocarbons or nitrogen-hydrogen complexes can generate even greater savings in energy consumption and carbon dioxide emission. These figures can be reduced to almost zero by the optimum combination or integration of processes. Thus, the energy from exothermic processes is used to supply endothermic processes in an energy neutral situation. Likewise, carbon dioxide emitted from one process is recycled to other processes, thus minimising or eliminating any excess carbon dioxide which has to be released into the atmosphere.
Integrating processes to make the Synthesis Gas with those to produce nitrogen-hydrogen complexes such as ammonia have the further advantage that both the major components of air, oxygen and nitrogen, are used in the integrated processes.
The following examples illustrate the possible scenarios of downstream processes. In the examples “Gasification/Reformer and Cleanup” refers to the “Reformer”, “Gasification”, “Stream Toxin Removal” and “Final Toxin Removal” steps in
All of the report mass balances are based on a feed of 100 mol/s of coal (simplified to its carbon content only) and can be scaled on this basis. The processes are designed to theoretically require only feed product interchange. This does not permit for the heat exchange inefficiencies.
These flow rates are indicative only and do not include the usual contaminants of a gasification and reformer process, namely H2S and mercury amongst others.
This simplified flow sheet also disregards the toxin removal steps as these are established and licensed technologies.
For the molar and mass balance shown in Tables 1 and 2, the product is characterised as an octane stream, this is representative of a product distribution corresponding to an alpha of between 0.86 and 0.88. For an alpha of between 0.84 and 0.86 (representative product Heptane) one would use the values in Tables 4 and 5, and for a value of between 0.81 and 0.84 one could use hexane as the representative product stream and obtain the values in Tables 7 and 8. The enthalpy flows are given in tables 2, 5 and 8 respectively. The unit energy loads are given in tables 3, 6 and 9.
The flows shown do not represent the actual vessel output flows but rather the system net flows from unit blocks to be expected in the process. This is necessary as the gross flows would depend on the specifics of the catalyst selection and vessel design. These detailed design parameters would influence the degree of water gas shift equilibrium as well as the product alkane/oxygenate distribution. The purpose of these examples is to provide a demonstration of the general theory of the present invention.
The theoretical carbon dioxide limits of conventional processes are as follows:
Comparing the theoretical carbon dioxide production in Table 10 with that produced in the processes according to the invention it will be noted that a great reduction in carbon dioxide emissions results from the processes of the invention.
For purposes of further comparison, Tables 1A, 2A and 3A below illustrate molar flows where a coal only feed is used according to prior art processes.
Comparing the figures in the Tables 1A, 2A and 3A to those in Tables 1, 2 and 3 illustrates that it is possible to reduce the carbon dioxide emissions by approximately half per molar unit of product produced by using the process of the present invention. This is both highly beneficial and unexpected.
The flows shown below do not represent the actual reactor output flows but rather the system net flows from unit blocks to be expected in the process. This is necessary as the gross flows would depend on the specifics of the catalyst selection and reactor design.
For a combination of process products there are two distinct process possibilities.
For product with less than 4.56 moles of Octane equivalent (alpha=0.86-0.88) per 100 moles of coal fed, the process diagram is given below as
The corresponding molar, mass and enthalpy flows are given in Tables 14, 15 and 16.
For product with greater than 4.56 moles of Octane equivalent (alpha=0.86-0.88) per 100 moles of coal fed, the process diagram is given below as
The corresponding molar, mass and enthalpy flows are given in Tables 17, 18 and 19.
Similar demonstrations can be shown for other alpha value as this will affect the composition of the feedstock and operation of the units.
It will be appreciated that the process conditions will be varied to take into account different feed materials and also to control the composition of the Synthesis Gas and products obtained therefrom.
It will further be apparent from the above examples that combining the products of the gasification reaction and reforming reaction result in a significant reduction in carbon dioxide emissions. This not only has great environmental benefits but also results in much greater process economies than can be achieved through conventional processes.
| Number | Date | Country | Kind |
|---|---|---|---|
| 20047676 | Mar 2005 | ZA | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/IB2006/000651 | 3/23/2006 | WO | 00 | 3/5/2008 |
