Method of Heat Management in Lpg Synthesis from Bio-Based Sources

The invention is related to synthesis of liquefied petroleum gas (LPG) from bio-based sources and a method of heat management therefor.

The issue of climate change is a real and growing problem. Carbon dioxide emissions from the burning of fossil fuels are a significant driving force. To address this issue various government regulations will soon require the use of renewable fuels as a component in conventional fuels, including propane and LPG. For example, the European renewable energy policy framework has just raised the EU target share of renewables to 40% by 2030.

The California Air Resources Board regulations require transportation fuel producers and importers to meet specified average carbon intensity requirements for fuel. Low Carbon Fuel Standard regulated fuels include natural gas, electricity, hydrogen, gasoline mixed with at least 10% corn-derived ethanol, biomass-based diesel, and propane.

Inland countries in Africa face a different issue. Propane and LPG are widely used as cooking fuels, but they must be imported and transported over land. This significantly increases their costs. Production of propane and LPG near the inland markets would be a cost savings, and, when produced from renewable resources, would also address climate change issues.

Thus, the demand for propane and LPG made from a non-fossil and/or renewable resources (bio-based propane and bio-based LPG) is real, current, and worldwide.

There are several other issues regarding the synthesis/conversion reaction sequence using synthesis gas as a reactant. In one, significant amounts of hydrogen are present in the exit gas from the reactor. While recycling has been proposed, conventional recycling processes involve recompression of the recycled hydrogen, at significant energy costs. Secondly, in conventional processing, over 10% of the carbon introduced as reaction feedstock is produced as carbon dioxide. This represents a waste of the valuable carbon monoxide resource in the bio-based synthesis gas. Accordingly, there continues to be a need for producing LPG from bio-based sources, using a sequence of processing steps that result in high LPG yields at low loss of the synthetic gas components, H, CO, and CO.

In one aspect, the present disclosure describes various embodiments of a system and a process for converting bio-based synthesis gas comprising CO and Hinto LPG. One source of the bio-based synthesis gas is light hydrocarbon gases, principally methane, that have been generated from and recovered from one or more biomass sources.

In another aspect, the present disclosure provides an improved process for converting synthesis gas to light (i.e., C3+) hydrocarbons, principally LPG, that has multiple uses as a biofuel source of power and heat.

In another aspect, the present disclosure provides an improved process for converting greenhouse gases, principally methane, into bio-based fuels that may be used as automotive, commercial, and domestic sources of heat and power with reduced, and in some cases, minimal environmental impact.

In another aspect, the present disclosure provides a process for converting hydrocarbon gases generated from agricultural and municipal sources, including wastewater and sewage treating and solids disposal sites, into low environmental impact fuels.

In another aspect, the present disclosure provides an improved process for producing LPG from a synthesis process while recovering and efficiently recycling the unreacted synthesis gas components. The improved process uses heat produced in the LPG synthesis in a separate endothermic reactor zone.

In another aspect, the present disclosure is directed to a method for producing bio-based LPG, comprising: a) reacting a bio-based synthesis gas in an exothermic reaction and forming an LPG-enriched effluent stream, wherein the exothermic reaction generates excess heat; b) increasing the enthalpy of a heat transfer fluid by absorbing at least a portion of the excess heat with the heat transfer fluid; c) supplying heat from the heat transfer fluid having increased enthalpy to an endothermic reaction and decreasing the enthalpy of the heat transfer fluid; d) returning the heat transfer fluid with decreased enthalpy to the exothermic reaction; and e) recovering the bio-based LPG from the LPG-enriched effluent stream.

In another aspect, the present disclosure is directed to a method for producing bio-based LPG, comprising: a) contacting a biogas comprising biomethane with an oxidizing gas selected from O, COand HO or combinations thereof at reforming reaction conditions in a reforming reaction zone to form a fresh bio-based synthesis gas; b) blending at least a portion of the fresh bio-based synthesis gas with a synthesis gas recycle stream to form a blended bio-based synthesis gas; c) reacting the blended bio-based synthesis gas in an oxygenate synthesis zone containing an oxygenate synthesis catalyst and forming a gaseous synthesis reaction product comprising oxygenates, wherein the oxygenates include at least 50 mol % methanol; d) reacting the gaseous synthesis reaction product in an oxygenate conversion zone containing oxygenate conversion catalyst and forming the LPG-enriched effluent stream; e) increasing the enthalpy of a heat transfer fluid by absorbing at least a portion of the excess heat generated in the exothermic oxygenate conversion reaction with the heat transfer fluid; f) supplying heat from the heat transfer fluid having increased enthalpy to an endothermic reaction and decreasing the enthalpy of the heat transfer fluid; and g) recovering the bio-based LPG and the synthesis gas recycle stream from the LPG-enriched effluent stream.

The fresh bio-based synthesis gas is prepared by contacting a biogas comprising biomethane with an oxidizing gas selected from O, COand HO or combinations thereof at reforming reaction conditions in a reforming reaction zone.

The method of synthesizing an LPG-enriched gaseous effluent may include a two-step reaction process, including a) reacting the blended bio-based synthesis gas in an oxygenate synthesis zone containing an oxygenate synthesis catalyst and forming an oxygenated reaction product comprising oxygenates and unreacted bio-based synthesis gas, wherein the oxygenates include at least 50 mol % methanol; and b) reacting at least a portion of the oxygenated reaction product in an oxygenate conversion zone containing an oxygenate conversion catalyst and forming the LPG-enriched gaseous effluent.

In effect, the disclosed embodiments of the present invention enable preparation of LPG from bio-based sources at high LPG yield and low loss of synthetic gas components H, CO, and COin the recycle process.

As used herein, “C2− hydrocarbons” refers to hydrocarbons composed of 1 or 2 carbon atoms (e.g., methane or ethane), either alone or in combination. Likewise, “C2+ hydrocarbons” refers to hydrocarbons composed of 2 or more carbon atoms (e.g., ethane, propane, etc.). Likewise, C3 hydrocarbons refers to hydrocarbons composed of 3 carbon atoms (e.g., propane). Likewise, C4 hydrocarbons refers to hydrocarbons composed of 4 carbon atoms (e.g., butane). Likewise, C4− hydrocarbons refers to hydrocarbons composed of 1 to 4 carbon atoms (e.g., methane, ethane, propane, and butane). Likewise, “C5+ hydrocarbons” refers to hydrocarbons composed of five or more carbon atoms (pentane, hexane, etc.).

As used herein, the term “LPG” refers to liquefied petroleum gas, a composition comprising a mixture of hydrocarbon gases, such as propane, propylene, butylene, isobutane, or n-butane. The term may refer to slightly different compositions, depending on the market to which the LPG is directed. For example, European LPG is a mixture of light hydrocarbons comprising propane and optionally n-butane and iso-butane. It is synonymous with AutoGas. Smaller amounts of ethane and C5+ may be present. In the United States, LPG mostly refers to propane. Bio-based LPG is LPG made from biogas.

As used herein, the terms “LPG and “bio-based LPG” are used interchangeably unless otherwise specified. According to the present disclosure, the composition of any LPG produced as described herein may be tailored by distillate fractionation; and the present process is suitable for producing LPG across a range of compositions. Thus, the term “LPG” as used herein refers to a mixture of propane and butane (n-butane and/or i-butane) in any composition ratio.

As used herein, “H”, “CO”, “CO”, “MeOH”, and “DME” have conventional designations, referring to molecular hydrogen, carbon monoxide, carbon dioxide, methanol, and dimethyl ether.

As used herein, a “bio-based” material refers to a material that is sourced from one or more natural resources, which will replenish to replace the portion depleted by usage and consumption, either through natural reproduction or other recurring processes in a finite amount of time in a human time scale.

As used herein, “biogas” refers to a gaseous material comprising methane containing carbon and/or hydrogen that is derived from bio-based resources. A biogas recovered from biomass processing may also comprise CO. In one aspect, biogas comprises methane and COin a molar ratio ranging from 80:20 to 20:80, or 70:30 to 30:70, or 60:40 to 40:60, or 50:50.

As used herein, “biomass” refers to solid or liquid material of biological origin or from municipal solid or liquid wastes, from agricultural solid and liquid wastes, from forestry products, or from any other natural products or waste such as seaweed or sea plants, including on-purpose agricultural products made for gasification, much of which are derived ultimately from materials having a biological origin.

As used herein, “syngas” or, in the alternative, “synthesis gas” refers to a mixture of Hand CO in various ratios. Syngas may also contain one or more of CO, CH, and HO.

As used herein, “oxygenate” refers to hydrocarbons containing oxygen. Examples include alcohols, such as methanol (MeOH) and dimethyl ether (DME). Biooxygenate, biomethanol and biodimethyl ether are these materials derived from bio-based synthesis gas.

As used herein, bio-based CO refers to CO containing carbon that is sourced from renewable sources, from biological sources, or from carbon capture process involving capture of CO and COfrom the atmosphere, from flue gas and the like.

As used herein, the terms “reaction zone temperature” and “catalyst temperature” refer to the average catalyst bed temperature during the catalytic reaction process. In one aspect, the catalyst temperature is a numerical average of the temperature of the operating catalyst bed at the feed inlet and the temperature of the operating catalyst bed at the product outlet.

As used herein, the term “molecular sieve” is a crystalline substance with pores of molecular dimensions which permit the passage of molecules below a certain size. It is commonly used as a commercial adsorbent and catalyst. Exemplary molecular sieves include phosphate molecular sieves (comprising silicon, aluminum, phosphorous, oxygen); and zeolites (comprising silicon, aluminum, and oxygen). Non-limiting examples of zeolitic molecular sieves include Beta zeolite, Y-zeolite, SSZ-13, or ZSM-5. In the context of a catalyst particle, “non zeolitic” refers to a catalyst containing no zeolites or phosphate molecular sieves, In the context of a catalyst bed, “non-zeolitic” refers to a bed of catalyst particles containing no zeolites or phosphate molecular sieves.

The gaseous feed to the reforming reaction zone comprises methane, in some cases with decreasing amounts of C2+ higher hydrocarbons, recovered from a source of biogas. Biogas that is generated for use according to the present disclosure contains biomethane or methane which is derived in part or in whole from a bio-based resource. Exemplary sources of bio-based methane include (i) methane obtained from anaerobic bacterial digestion of agricultural waste, municipal biowastes or from wastewater treatment, (ii) gaseous products of biomass conversion (e.g., composting, biomass gasification, pyrolysis, or hydropyrolysis, such as in the case of supercritical water gasification of biomass), (iii) landfill gases, or (iv) gaseous products of the electrochemical reduction of carbon dioxide. Carbon from bio-based carbon sources is termed “bio-based carbon”.

In some aspects, hydrogen may be added in the process to, for example, adjust the H/(CO+CO) content of a synthesis gas feed. Suitable hydrogen sources may include petroleum processing. Alternatively, bio-based hydrogen may be sourced from renewable sources, from biological sources, from electrolysis of water using solar, wind, wave, or other renewable energy sources or from naturally occurring geological hydrogen (commonly referred to as natural, gold or white hydrogen) or from nuclear powered water electrolysis (commonly referred to as pink hydrogen). Bio-based hydrogen is not, in general, formed by reactions of carbon compounds by steam reforming of methane.

Biogas may also contain CO, CO, ethane, water vapor, and nitrogen, depending on the specific process from which the biogas is generated. Raw (untreated) biogas may be passed to a reforming process without further treatment. Alternatively, non-methane components may be removed, either in part or in whole, and the treated biogas passed to the reformer for conversion into bio-based synthesis gas. Water that is present in the raw biogas may be condensed and removed from the biogas, using, for example, a water knockout pot for the two-phase separation. Non-hydrocarbon compounds (such as sulfur-, or nitrogen-, or acid-containing compounds) that are present in the raw biogas are removed to low levels, and often to ppm levels, using, for example, one or more of aqueous washing, alkanolamine absorption, molecular sieve adsorption, selective catalytic oxidation, and hydrodesulfurization.

Carbon dioxide may be removed from the raw biogas in combination with sulfur removal. Additional COmay be removed by membrane separation, by cryogenic distillation or by aqueous absorption, which includes contacting the biogas with water or caustic solutions to dissolve CO, separating the water/COmixture, removing the COfrom the mixture by increasing the temperature and/or decreasing the pressure of the mixture, and recycling the water. COmay also be removed in part by aqueous absorption into the water that is condensed and removed from the biogas. In some embodiments, at least a portion of one or more of CO, CO and water vapor may be retained in the treated biogas feed to maintain the desired H/(CO+CO) ratio of the bio-based synthesis gas exiting the reformer.

Carbon dioxide and/or water may also be added to the biogas feed from an external source to the reformer to control the H/(CO+CO) ratio in the bio-based synthesis gas produced in the reformer. In embodiments, carbon in the added carbon dioxide is from a bio-based resource, with the addition of carbon from a bio-based resource controlled to maintain a biogas carbon content of, for example, at least about 70 weight % that is bio-based carbon not derived from petroleum.

Recycle gas comprising H, CO, COand optionally methane and traces of C2+ hydrocarbons may also be added to the biogas, prior to passing the biogas as feed to the reforming reaction zone.

Bio-based synthesis gas comprising Hand CO may be produced by contacting a biogas comprising biomethane with an oxidizing gas selected from O, COand HO or combinations thereof at reforming reaction conditions in a reforming reaction zone to produce a bio-based synthesis gas comprising Hand CO.

Bio-based synthesis gas may be produced by biomass gasification, involving contacting biomass with some combination of air, oxygen, and/or steam at elevated temperatures. Fluidized-bed, fixed-bed or indirect heated gasifiers may be used. Varying steam to oxygen ratio input is a way to adjust the H/(CO+CO) ratio to match synthesis gas requirements. Gasifier temperatures may be between about 1,000° C. and about 1,300° C. or higher in some operations.

In another aspect, syngas (or alternatively bio-based synthesis gas) may be produced in a methane reformer involving steam reforming, autothermal reforming or partial oxidation to convert methane to hydrogen and carbon oxide gases. Either a fired biogas reformer or an electrical biogas reformer may be used. Reforming conditions include pressures between about 200 psi and about 600 psi (14-40 bar) and outlet temperatures between about 815° C. and about 925° C. Because the catalyst is sensitive to sulfur, the sulfur content of the biogas must be reduced to less than 10 ppm, preferably less than 1 ppm.

In steam methane reforming, steam reacts with methane as follows:

In the absence of steam, dry reforming proceeds as follows:

The reactants in the reforming reaction zone may also be converted by a water gas shift (WGS) reaction over the metal reforming catalysts (e.g., shaped nickel alumina catalysts):

Therefore, adjusting the amount of COand HO added to the methane reforming reaction zone feed is useful for controlling the H/(CO+CO) ratio of the syngas generated during reforming. The composition of syngas generated in the reforming reaction zone, and in particular the H/(CO+CO) ratio in the syngas, may be controlled for efficient downstream conversion of the syngas to LPG. When the ratio is too low CO conversion is reduced. When it is too high large quantities of Hmust be recycled. Synthesis of oxygenates in the oxygenate synthesis zone generally proceeds with a H/(CO+CO) molar ratio in the oxygenate synthesis zone feed in a range between 1 and 4 (e.g., in a range between 2 and 3). When the feed contains less than or equal to 1 mol % CO, the H/(CO+CO) ratio may be in a range between 2.25 and 2.45. When the feed contains more than 1 mol % COthe H/(CO+CO) ratio may be in the range of 2.2 to 2.5.

For managing control of environmental emissions from the process, additional COmay be added to the gaseous feed to the reforming reaction zone. In embodiments, the COused in the reformer is recovered either from the biogas generation reactor, from the recycle of unreacted products from the process, or from both. In particular, biogas generated from biomass includes COthat may be removed from the biogas as a pure COproduct, making it highly suitable for blending into the blended synthesis gas feed to the oxygenate synthesis zone. Thus, in some cases, the synthesis gas feed may further comprise CO, for example in an amount of at least about 5 mol % (e.g., between about 4-50 mol % or between about 7-25 mol % or between about 8-10 mol %).

Controlling for the amount of water supplied to the oxygenate synthesis zone may also influence the synthesis reactions in the oxygenate synthesis zone. In particular, the addition of steam to the reaction zone, and the reaction of the steam with CO by WGS that is generated in a reforming reaction step in the oxygenate synthesis zone increases the H/(CO+CO) in the reaction zone. Likewise, increasing the COintroduced to the oxygenate synthesis zone decreases the H/(CO+CO) by RWGS (reverse WGS).

Methane reforming for generating synthesis gas is generally conducted with a methane rich feed, comprising little or no C2+ components. Processes using a biogas feedstock containing excess C2+ hydrocarbons may include a pre-reformer for converting the C2+ hydrocarbons to methane. In embodiments, a primary source of C2+ components in the biogas feedstock is the light fraction recycle from the product recovery step. Suitable pre-reforming systems are known and are readily available.

Fresh bio-based synthesis gas that is supplied to an LPG oxygenate synthesis zone includes the bio-based synthesis gas produced in the reforming reaction zone. Other suitable sources of bio-based synthesis gas include one or more recycle streams generated in the process. Additional CO and/or H, some or all of which may be bio-based CO and/or bio-based Hmay be supplied from external sources. Syngas can also be produced in the endothermic reaction zone by the conversion of COand Hto CO and HO by the reverse water gas shift reaction.

The process, according to the present invention, is directed at least in part to producing an LPG-enriched gaseous effluent by a catalytic synthesis process. In one aspect, the method comprises synthesizing an LPG-enriched gaseous effluent by converting a blended bio-based synthesis gas in one or more catalytic reaction zones. The blended bio-based synthesis gas is prepared by blending treated synthesis gas recycle stream and fresh bio-based synthesis gas. In one aspect, the volume ratio of recycled syngas to fresh syngas may be between 1 and 15, or between 2 and 8.

The synthesis catalyst comprises at least one oxygenate synthesis catalyst for converting the bio-based synthesis gas into oxygenates such as methanol, and an oxygenate conversion catalyst for converting the oxygenates into hydrocarbons, including LPG.