Integrated Coal Liquefaction, Petroleum or Biomass Facility with Decreased Carbon Dioxide Production and Higher Carbon and Thermal Efficiencies

Abstract

The integration of hydrogen and methanol production within a coal liquefaction, petroleum refinery or biomass conversion facility resulting in the unanticipated benefits of lower carbon dioxide (CO.sub.2) production, net emissions, and higher carbon and thermal efficiencies is the subject of this invention.

Claims

1. A integrated process for simultaneously reducing carbon dioxide (CO.sub.2) production and net CO.sub.2 emissions while improving the carbon and thermal efficiencies of a heavy hydrocarbon processing facility comprising: (a) producing a high purity hydrogen stream and a methanol stream using a steam methane reformer and methanol production unit; (b) feeding a portion of said hydrogen stream to a hydrocracking unit that is processing a heavy hydrocarbon stream to create a liquids stream; (c) feeding a portion of said methanol stream and said hydrogen stream from step a) along with said liquids stream from step b) to a liquids upgrading unit to create one or more saleable petroleum streams.

2. The process of claim 1 wherein the hydrocarbon processing facility is a coal liquefaction plant.

3. The process of claim 1 wherein the hydrocarbon processing facility is a biomass plant.

4. The process of claim 1 wherein the hydrocarbon processing facility is a petroleum plant.

5. The process of claim 1 wherein the carbon emissions for the hydrocarbon processing facility as expressed per one thousand barrels of liquid product produced, are reduced by at least eight percent (8%).

6. The process of claim 1 wherein the carbon emissions for the hydrocarbon processing facility as expressed per one thousand barrels of liquid product produced, are reduced by at least five percent (5%).

7. The process of claim 1 wherein the carbon efficiency for the heavy hydrocarbon processing facility as expressed as the percentage of feed carbon to liquid product produced, is increased by at least one and one half percentage points (1.5%).

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0008] FIG. 1 shows a block flow diagram for the invention using a coal liquefaction facility as an example to illustrate Applicant's invention.

DETAILED DESCRIPTION OF THE INVENTION

[0009] FIG. 1 illustrates Applicant's processing configuration as applied in a coal liquefaction facility. Feed coal 10 is fed to coal preparation 20 for drying and sizing and then to the direct coal liquefaction complex 30, which includes one or more coal liquefaction reactors. Direct coal liquefaction (DCL) is a process that reacts coal 10 in a solvent (not shown) with hydrogen at high temperature and pressure to produce liquid fuels. In the coal liquefaction complex 30, the coal is converted using a solid extrudate catalyst (not shown) and hydrogen 22a to raw liquid 38 and gaseous 36 products. The aforementioned hydrogen stream 22a for the coal liquefaction unit is created in a steam methane reformer and methanol synthesis complex 16.

[0010] Reforming of natural gas with steam is referred to as steam methane reforming (SMR) and is an efficient and effective method of producing commercial bulk hydrogen. In Applicant's invention the steam methane reformer and methanol synthesis complex 16 comprises a steam reformer reactor unit (not shown), a furnace section (not shown), and a methanol production unit. Details concerning the steam methane reformer and methanol synthesis complex 16 are not shown in FIG. 1 but can be described as follows.

[0011] The steam methane reformer reactor unit operates at high temperatures (700-1100 C.) and in the presence of a metal-based catalyst. In the steam reformer reactor unit, a steam stream 2 reacts with the hydrocarbons in the natural gas 4 to yield carbon monoxide and hydrogen according to the following formula:

C.sub.nH.sub.2n+2+nH.sub.2O.fwdarw.nCO+(2n+1)H.sub.2

[0012] Other reactions occurring in the steam reformer reactor unit include the water gas shift according to the formula:

CO+H.sub.2O.fwdarw.CO.sub.2+H.sub.2

[0013] The primary SMR reaction is highly endothermic and requires high temperatures to obtain acceptable methane conversion rates. The large energy requirement for the SMR process is obtained from combustion reactions occurring in the furnace section of the steam reformer complex. The product from the steam reformer reactor unit is a synthetic gas stream, also known as syngas (not shown) containing primarily CO, CO.sub.2, H.sub.2, H.sub.2O and unreacted CH.sub.4.

[0014] The raw SMR syngas is routed to a methanol production unit where the carbon monoxide and carbon dioxide react, using a catalyst, to produce methanol and water. The reaction is exothermic and excess energy can be used to reduce the SMR reactor fuel requirements. Consistent with the high rate of synthesis gas due to the relatively large amount of hydrogen consumed in the subject invention, the methanol synthesis plant is once-through (i.e., no recycle).

[0015] The purge syngas from the methanol plant, containing the same components as in the SMR raw gas, is routed to the shift conversion unit. In the shift unit, the carbon monoxide is shifted to hydrogen with accompanying additional carbon dioxide production. The product gas from the shift conversion unit is sent to the carbon dioxide removal unit which selectively adsorbs carbon dioxide 28 from the gas. The hydrogen-rich product from the CO.sub.2 adsorber unit is further purified in a final membrane or adsorption unit resulting in hydrogen product 22. The hydrogen 22 gas contains in excess of 99 V % hydrogen and is thereafter available for use in the primary conversion and secondary upgrading units. The carbon dioxide stream 28 is thereafter further purified and compressed and is a final product.

[0016] A portion of the methanol 26 and a portion of the hydrogen 22b from the SMR/Methanol complex 16 is routed, along with liquid products 38 from the coal liquefaction complex 30 to the liquid upgrading unit 48 to produce saleable fuel products including, for example, M15 gasoline, 56, diesel 57, and vacuum gas oil (VGO) 58 products. The portion of the methanol stream 26 not utilized in the liquid upgrading unit 48 is exported 26b as a final product.

[0017] The raw gaseous products 36 from the coal liquefaction complex 30 are sent, along with raw gaseous products 55 from the liquid upgrading plant 48 to a light ends recovery unit 50 to produce, for example, fuel gas 52 and liquefied petroleum gases (LPG) 54, including propane, butane and mixtures thereof for use as refining fuel or as net products. Heavier components recovered in the light ends recovery section 50, shown as stream 51 are blended back to the liquid upgrading unit 48, primarily for M15 gasoline production.

[0018] This invention will be further described and understood by the following example case, which should not be construed as limiting the scope of the invention.

Example

Direct Coal Liquefaction Study

[0019] A U.S. based direct coal liquefaction facility was studied to illustrate the advantages of the invention. The commercial size facility processes 8,000 MTPD (dry basis) of a bituminous coal to produce saleable liquid fuels. Three commercial cases were developed to estimate overall plant yields and economics including profitability. The first two cases (1 and 2) do not have any methanol production. In all cases, the coal is liquefied in a high pressure, high temperature ebullated-bed reactor system and the products are treated to be saleable. Electric power is imported in all cases except Case 1 where power is generated in the facility. A portion of the carbon dioxide from the SMR or gasifier (used in Case 1 only) is captured, purified and compressed.

[0020] The three cases are described below:

[0021] Case 1The hydrogen requirements for the primary conversion and hydrotreating units are provided by the steam-oxygen gasification of the unconverted coal from the liquefaction unit and additional fresh coal. There is no methanol production. There is no SMR unit. An air separation plant is included with this case to produce the oxygen for the gasifier.

[0022] Case 2The hydrogen requirements are provided by a natural gas fed SMR instead of the gasifier. There is no methanol production. The direct coal heavy residue, including unconverted coal and ash, is sent to the plant's battery limits for sale as a fuel.

[0023] Case 3This case is the same as Case 2 except that the SMR raw gas is first routed to methanol production. This is the process configuration which utilizes the Applicant's invention. The production rate of methanol product is sufficient to provide a M15 gasoline product and methanol export.

[0024] The technical and economic results of the commercial study are summarized in Tables 2 and 3. Important assumptions are shown in Table 1 below.

TABLE-US-00001 TABLE 1 Important Assumptions Item Units Value Timeframe 2017 Operation per Year Days 330 Construction Period Years 3 Coal Cost $/Short Ton 27 Light Oil (Brent) Price $/Bbl 70 Natural Gas Price $/MM Btu 2.5 Power Cost $/Kw-Hr 0.055 Methanol Value S/Bbl 47

[0025] The two base cases (1 and 2) illustrate the difference between SMR and gasification for the production of the required hydrogen. The carbon dioxide captured is higher for the gasification case, however the carbon efficiency (fraction of feed carbon to liquid products) is significantly lower (57 vs. 49%). The carbon emitted to the atmosphere is also much higher for the gasification case. The gasification case has higher investment and significantly lower IRR. The lower profitability, relative to SMR based hydrogen production, is typically evident at natural gas prices lower than approximately $10/MM Btu.

[0026] The production of M15 gasoline and export of excess methanol in Case 3 has a higher level of carbon efficiency than Case 2 (58.5 vs. 57.0%), indicating that the incremental production of methanol is an efficient use of natural gas and will result in lower carbon dioxide production per quantity of liquids produced. This is shown in Table 2 where the carbon dioxide emitted is expressed per 1000 barrel of liquid product, the carbon emissions are 8% lower (92.6 vs. 100.6 ST/1000 Bbl) for Case 3 relative to Case 2. This is a significant outcome of the invention. There is also a 1.4 percentage point increase in the overall plant thermal efficiency relative to Case 2.

[0027] Relative to Case 2, Case 3 has 21% higher liquids production. This due to 6,357 BPSD of methanol production with 1,968 BPSD used to produce M15 gasoline and 4,389 BPSD exported. As shown in Table 3, Case 3 has a significantly larger plant annual net margin ($516 vs. $416 MM) and a higher project profitability. These economic results are also important outcomes of the study.

TABLE-US-00002 TABLE 2 Technical Results Case 1 Case 2 Case 3 Coal Feed, MF STPD To Liquefaction 8,000 8,000 8,000 To Gasification 3,022 Net 11,022 8,000 8,000 Natural Gas Feed, MMSCFD 74.2 98.3 Power, kW 0 98 100 Liquids, BPSD C.sub.3/C.sub.4 3,039 3,039 3,025 Gasoline 11,074 11,074 13,122 Methanol in Gasoline 1,968 Diesel 14,197 14,197 14,197 VGO Fuel 2,819 2,819 2,819 Net Product Methanol 4,389 Total Liquids 31,129 31,129 37,553 Liquids, B/ST of Coal 2.82 3.89 4.69 Carbon Dioxide, STPD Captured 11,062 2,851 2,699 Emitted 3,591 3,131 3,476 Total 14,653 5,982 6,175 Carbon Dioxide Emitted, ST/1000 Bbl of Liquid 115.4 100.6 92.6 Carbon Efficiency - % Feed Carbon 49.3 57.0 58.5 to Liquid Products Overall Thermal Efficiency, % 59.4 73.7 75.1

TABLE-US-00003 TABLE 3 Economic Results Case 1 Case 2 Case 3 Operating Cost, $MM/Yr Fixed 268 181 187 Variable 171 233 254 Total 439 414 441 Revenues, $MM/Yr 830 830 957 Coal Feedstock Costs, $MM/Yr 110 80 80 Net Margin, $MM/Yr 391 416 516 Investment, $MM 4,669 3,145 3,264 % of base 100.0 67.4 69.9 Pre-Tax IRR, % 4.7 9.5 11.7 Relative to Base, Abs % +4.8 +7.0

[0028] The invention described herein has been disclosed in terms of specific embodiments and applications. However, these details are not meant to be limiting and other embodiments, in light of this teaching, would be obvious to persons skilled in the art. Accordingly, it is to be understood that the drawings and descriptions are illustrative of the principles of the invention, and should not be construed to limit the scope thereof.