CN114531875A - On-line process for treating wax-containing crude methanol stream - Google Patents
On-line process for treating wax-containing crude methanol stream Download PDFInfo
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- CN114531875A CN114531875A CN202080050739.7A CN202080050739A CN114531875A CN 114531875 A CN114531875 A CN 114531875A CN 202080050739 A CN202080050739 A CN 202080050739A CN 114531875 A CN114531875 A CN 114531875A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 609
- 238000000034 method Methods 0.000 title claims abstract description 100
- 230000008569 process Effects 0.000 title claims description 36
- 238000001816 cooling Methods 0.000 claims abstract description 112
- 239000007788 liquid Substances 0.000 claims abstract description 89
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 28
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 14
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 14
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 14
- 239000001257 hydrogen Substances 0.000 claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 14
- 238000012545 processing Methods 0.000 claims abstract description 8
- 239000012530 fluid Substances 0.000 claims description 61
- 239000012188 paraffin wax Substances 0.000 claims description 61
- 238000004891 communication Methods 0.000 claims description 59
- 230000002209 hydrophobic effect Effects 0.000 claims description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- 229910052757 nitrogen Inorganic materials 0.000 claims description 10
- 239000002826 coolant Substances 0.000 claims description 4
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 19
- 230000015572 biosynthetic process Effects 0.000 abstract description 10
- 238000003786 synthesis reaction Methods 0.000 abstract description 10
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 description 23
- 239000000047 product Substances 0.000 description 23
- 238000004140 cleaning Methods 0.000 description 16
- 239000001993 wax Substances 0.000 description 9
- 150000002431 hydrogen Chemical class 0.000 description 8
- 238000010926 purge Methods 0.000 description 8
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical group CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 6
- DCAYPVUWAIABOU-UHFFFAOYSA-N hexadecane Chemical compound CCCCCCCCCCCCCCCC DCAYPVUWAIABOU-UHFFFAOYSA-N 0.000 description 6
- 238000005201 scrubbing Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- 239000006227 byproduct Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 3
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 239000003849 aromatic solvent Substances 0.000 description 3
- WJTCGQSWYFHTAC-UHFFFAOYSA-N cyclooctane Chemical compound C1CCCCCCC1 WJTCGQSWYFHTAC-UHFFFAOYSA-N 0.000 description 3
- 239000004914 cyclooctane Substances 0.000 description 3
- -1 hexadecane) Chemical class 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 150000001924 cycloalkanes Chemical class 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000011261 inert gas Substances 0.000 description 2
- 239000003960 organic solvent Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
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- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000003225 biodiesel Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 239000006184 cosolvent Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000005764 inhibitory process Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005809 transesterification reaction Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
- B01D5/0072—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with filtration
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/1516—Multisteps
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/78—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by condensation or crystallisation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/86—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment
Abstract
Systems and methods for processing crude methanol are disclosed. A crude methanol stream comprising methanol and paraffins is produced from synthesis gas (carbon monoxide, carbon dioxide and hydrogen). The crude methanol stream is cooled to form a partially condensed crude methanol stream, which is further separated in a gas-liquid separator to form a liquid stream and a gas stream. The liquid stream is further cooled in a dewaxing unit to remove paraffins. The dewaxing unit includes two or more cooling units arranged in parallel so that the methanol system does not need to be shut down when one of the cooling units is cleaned off-line.
Description
Cross Reference to Related Applications
This application claims priority from U.S. provisional patent application No. 19175454.8, filed on 2019, month 5, and day 20, the entire contents of which are incorporated herein by reference in their entirety.
Technical Field
The present invention relates generally to systems and methods for producing methanol. More particularly, the present invention relates to a system and method for removing paraffin wax produced as a byproduct in a methanol production plant using cooling devices in parallel.
Background
Methanol is a colorless, flammable solution that can be used in many chemical processes and industrial classes. Methanol can be used as a raw material for producing formaldehyde which is widely used for producing polymers. Methanol can also be passed through various catalytic processes to produce olefins and gasoline. Methanol can also be used to produce biodiesel via transesterification with glycerol. In addition, methanol is used as a co-solvent mixed in gasoline or directly as a fuel.
Currently, the most widely used process in methanol production involves a catalytic reaction between carbon monoxide, carbon dioxide and hydrogen. In this process, by-products including paraffins are produced and mixed with methanol. The paraffin wax is subsequently removed by a cooler. During cooling, paraffin wax may deposit in the tubes of the cooler, resulting in a reduction in the heat transfer coefficient and overall cooling capacity of the cooler. Due to the increasing thickness of paraffin deposits and thus the inability to sustain methanol production capacity, the methanol production system has to be shut down to perform the chiller cleaning process, resulting in lost production days and reduced overall system run time.
In general, despite the existence of systems and methods for producing methanol, there is still a need for improvement in this area in view of the shortcomings of at least these methods.
Disclosure of Invention
A solution to the above-mentioned problems associated with methanol production processes using synthesis gas (hydrogen, carbon monoxide and carbon dioxide) has been found. The solution consists in a method for treating crude methanol produced using synthesis gas. The method includes cooling a crude methanol stream to produce a liquid stream comprising crude methanol and paraffin wax, and further cooling the liquid stream in a dewaxing unit comprising two or more cooling units arranged in parallel with each other. This is at least advantageous for controlling each cooling unit individually so that when one of the cooling units is cleaned off-line, the other cooling unit can be operated to maintain the operation of the entire methanol production system. Therefore, the method can prevent the methanol production system from being completely shut down due to the need to remove the paraffin accumulated in the cooling device. Thus, the process can reduce or eliminate the loss of production time experienced by conventional methanol production systems and processes. Accordingly, the process of the present invention provides a technical solution to at least some of the problems associated with the above-described conventional systems and processes for producing methanol.
Embodiments of the invention include methods of treating crude methanol comprising paraffin wax. The method includes treating a crude methanol stream to produce a first liquid stream comprising substantially simultaneously water, methanol, and paraffin. The method also includes sending the first liquid stream to a dewaxing device. The dewaxing device comprises (a) a feed inlet and (b) a first cooling device and a second cooling device which are arranged in parallel. The dewaxing device is configured such that the dewaxing device feed is in fluid communication with the first cooling device, the second cooling device, or both. The fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing device feed and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed and the second cooling device. The process also includes separating the first liquid stream in a dewaxing device to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream.
Embodiments of the invention include methods of treating crude methanol comprising paraffin wax. The method includes treating a crude methanol stream to produce a first liquid stream comprising primarily simultaneously water, methanol, and paraffin. The dewaxing unit includes a dewaxing unit feed inlet. The dewaxing device also comprises a first cooling device and a second cooling device which are arranged in parallel. The dewaxing device is configured such that the dewaxing device feed is in fluid communication with the first cooling device, the second cooling device, or both. The fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing device feed and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed and the second cooling device. The dewaxing apparatus also includes (1) a filter feed and (2) a first hydrophobic filter and a second hydrophobic filter disposed in parallel with each other. The dewaxing device is configured such that the filter feed is in fluid communication with the first hydrophobic filter, the second hydrophobic filter, or both. The fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing unit feed and the first hydrophobic filter, and/or one or more valves between and/or in fluid communication with the dewaxing unit feed and the second hydrophobic filter. The process also includes separating the first liquid stream in a dewaxing device to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream.
Embodiments of the invention include methods of treating crude methanol comprising paraffin wax. The method includes delivering a crude methanol stream comprising paraffin wax to a heat exchanger. The process also includes cooling the crude methanol stream through a heat exchanger to form a cooled crude methanol stream having a temperature of 120 ℃ to 135 ℃ and/or comprising 94 vol% to 98 vol% vapor. The process also includes passing the cooled crude methanol stream to a first condenser. The process further includes cooling the cooled crude methanol stream in a first condenser to form a partially condensed stream having a temperature of from 72 ℃ to 80 ℃ and/or comprising from 86% to 90% by volume vapor. The method also includes passing the partially condensed stream to a first separator. The process further includes separating the partially condensed stream by a first separator to form at least (1) a first vapor stream comprising one or more of hydrogen, carbon monoxide, carbon dioxide, methane, nitrogen, uncondensed methanol, and water; and (2) a first liquid stream comprising substantially simultaneously water, methanol and paraffin. The method also includes conveying the first vapor stream to a second condenser. The process also includes cooling the first vapor stream in a second condenser to form a cooled first vapor stream having a temperature of 45 ℃ or less than 45 ℃. The process also includes passing the cooled first vapor stream to a second separator. The process also includes separating the cooled first vapor stream by a second separator to form at least (1) a second vapor stream comprising one or more of syngas, nitrogen, and methane and (2) a second liquid stream comprising primarily methanol. The method also includes sending the first liquid stream to a dewaxing device. The dewaxing unit includes a dewaxing unit feed inlet. The method further comprises a first cooling device and a second cooling device arranged in parallel with each other. The dewaxing device is configured such that the dewaxing device feed is in fluid communication with the first cooling device, the second cooling device, or both. The fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing device feed and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed and the second cooling device. The dewaxing apparatus also includes a filter feed. The dewaxing apparatus also includes a first hydrophobic filter and a second hydrophobic filter disposed in parallel with each other. The dewaxing device is configured such that the filter feed is in fluid communication with the first hydrophobic filter, the second hydrophobic filter, or both. The fluid communication is controlled by one or more valves between and/or in fluid communication with the filter feed port and the first hydrophobic filter, and/or by one or more valves between and/or in fluid communication with the filter feed port and the second hydrophobic filter. The process also includes separating the first liquid stream in a dewaxing device to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream comprising primarily methanol.
The following includes definitions of various terms and phrases used throughout this specification.
The term "about" or "approximately" is defined as being approximately as understood by one of ordinary skill in the art. In one non-limiting embodiment, the term is defined as a range that is within 10%, preferably within 5%, more preferably within 1%, and most preferably within 0.5%.
The terms "weight%", "volume%" or "mole%" refer to the percentage of the weight, volume or moles, respectively, of a component in the total weight, volume or moles of the material comprising the component. In one non-limiting example, 10 moles of a component in 100 moles of material is 10 mole percent of the component.
The term "substantially" and variations thereof are defined as being within 10%, within 5%, within 1%, or within 0.5%.
The terms "inhibit" or "reduce" or "prevent" or "avoid" or any variation of these terms, when used in the claims and/or the specification, includes any measurable reduction or complete inhibition to achieve the intended result.
The term "effective" when used in the claims and/or specification is sufficient to achieve a desired, expected, or expected result.
When used in the claims or specification with the word "comprising," including, "" containing, "or" having, "the singular forms of an element may mean" a, "" an, "or" one, "but the plural is also intended to mean" one or more, "" at least one, "and" one or more than one.
The terms "comprising," "having," "including," or "containing" are inclusive or open-ended and do not exclude additional, unrecited elements or method steps.
The methods of the present invention may "comprise," consist essentially of, "or" consist of the particular materials, ingredients, compositions, etc. disclosed throughout this specification.
The term "predominantly" when used in the claims and/or specification refers to any one of greater than 50 weight percent, 50 mole percent, and 50 volume percent. For example, "predominantly" can include from 50.1% to 100% by weight and all ranges and values therebetween, from 50.1% to 100% by mole and all ranges and values therebetween, or from 50.1% to 100% by volume and all ranges and values therebetween.
Other objects, features and advantages of the present invention will become apparent from the drawings, detailed description and examples which follow. It should be understood, however, that the drawings, detailed description and examples, while indicating specific embodiments of the present invention, are given by way of illustration only and not by way of limitation. It is further contemplated that various changes, combinations, and modifications within the spirit and scope of the invention will become apparent to those skilled in the art from this detailed description. In other embodiments, features from specific examples may be combined with features from other examples. For example, features from one embodiment may be combined with features from any of the other embodiments. In other embodiments, additional features may be added to the specific embodiments described herein.
Drawings
For a more complete understanding, reference is now made to the following descriptions taken in conjunction with the accompanying drawings, in which:
FIG. 1A shows a schematic diagram of a system for producing methanol including a gas-liquid separator for separating the effluent of a methanol synthesis unit, according to an embodiment of the present invention;
FIG. 1B shows a schematic diagram of a system for producing methanol including a methanol wash column for separating the effluent of a methanol synthesis unit, according to an embodiment of the present invention;
FIG. 2 shows a schematic diagram of a dewaxing heat exchanger of a dewaxing unit according to an embodiment of the present invention; and
fig. 3 shows a schematic diagram of a method of treating crude methanol according to an embodiment of the present invention.
Detailed Description
Currently, methanol is produced by the catalytic reaction of carbon monoxide, carbon dioxide and hydrogen. The resulting crude methanol, including the by-product paraffin, is then condensed in a series of cooling units to remove the paraffin and purify the methanol. However, since paraffin is gradually deposited in the cooling device, the heat transfer coefficient and cooling capacity of the cooling device are reduced to such an extent that the productivity of dewaxing crude methanol cannot meet the production requirements. Typically, to clean the cooling unit, the entire methanol production system must be shut down, resulting in loss of production time and run time of the production system. The present invention provides a solution to at least the problems. The solution is premised on a method of treating crude methanol comprising cooling crude methanol produced using syngas by two or more cooling units arranged in parallel with each other, such that when one of the cooling units is taken off-line, e.g. cleaned, the system can be maintained in operation by using the other cooling units in the system. Therefore, the total production time and operation time of the methanol production system can be improved as compared with the conventional method, and the productivity of methanol can be increased as compared with the conventional method. This and other non-limiting aspects of the present invention are discussed in further detail in the following sections.
A. Methanol production system
In an embodiment of the invention, a system for producing methanol includes a methanol synthesis unit, a dewaxing unit, and one or more gas-liquid separators. Referring to fig. 1A, there is seen a schematic diagram of a system 100 that is capable of continuously producing methanol without system shut-down due to paraffin build-up in the dewaxing unit. According to the embodiment of the inventionThe system 100 may include a methanol synthesis unit 50 that may react the hydrogen of the heated feed stream 76 with carbon monoxide and carbon dioxide to produce a product stream 77 comprising crude methanol. The crude methanol may include methanol; paraffin wax; water; other by-products (e.g., ethanol); unreacted synthesis gas including carbon monoxide, carbon dioxide, hydrogen, methane and inert gases (e.g., nitrogen); or a combination thereof. The paraffin wax may comprise C18Paraffin (C)18H38) To C60Paraffin (C)60H122). In an embodiment of the present invention, the methanol synthesis unit 50 includes a catalyst comprising CuO, ZnO, Al2O3Or a combination thereof. In embodiments of the invention, the temperature of the heated feed stream 76 is 165 ℃ to 180 ℃ and all ranges and values therebetween, including 165 ℃ to 166 ℃, 166 ℃ to 167 ℃, 167 ℃ to 168 ℃, 168 ℃ to 169 ℃, 169 ℃ to 170 ℃, 170 ℃ to 171 ℃, 171 ℃ to 172 ℃, 172 ℃ to 173 ℃, 173 ℃ to 174 ℃, 174 ℃ to 175 ℃, 175 ℃ to 176 ℃, 176 ℃ to 177 ℃, 177 ℃ to 178 ℃, 178 ℃ to 179 ℃, and 179 ℃ to 180 ℃. The temperature of the product stream 77 can be 205 ℃ to 235 ℃ and all ranges and values therebetween, including 205 ℃ to 207 ℃, 207 ℃ to 209 ℃, 209 ℃ to 211 ℃, 211 ℃ to 213 ℃, 213 ℃ to 215 ℃, 215 ℃ to 217 ℃, 217 ℃ to 219 ℃, 219 ℃ to 221 ℃, 221 ℃ to 223 ℃, 223 ℃ to 225 ℃, 225 ℃ to 227 ℃, 227 ℃ to 229 ℃, 229 ℃ to 231 ℃, 231 ℃ to 233 ℃, and 233 ℃ to 235 ℃. The pressure of product stream 77 may be 80kg/cm2To 110kg/cm2And all ranges and values therebetween, including 80kg/cm2To 82kg/cm2、82kg/cm2To 84kg/cm2、84kg/cm2To 86kg/cm2、86kg/cm2To 88kg/cm2、88kg/cm2To 90kg/cm2、90kg/cm2To 92kg/cm2、92kg/cm2To 94kg/cm2、94kg/cm2To 96kg/cm2、96kg/cm2To 98kg/cm2、98kg/cm2To 100kg/cm2、100kg/cm2To 102kg/cm2、102kg/cm2To 104kg/cm2、104kg/cm2To 106kg/cm2、106kg/cm2To 108kg/cm2And 108kg/cm2To 110kg/cm2。
According to an embodiment of the invention, the system 100 may include a feed effluent heat exchanger 51 configured to cool the product stream 77 to produce a first cooled product stream 78, and to heat the feed stream 75 to produce a heated feed stream 76. In an embodiment of the invention, the outlet of the feed effluent heat exchanger 51 is in fluid communication with the inlet of the cooler 52 such that the first cooled product stream 78 flows from the feed effluent heat exchanger 51 to the cooler 52. In an embodiment of the invention, cooler 52 is configured to cool first cooled product stream 78 to produce second cooled product stream 79. The temperature of the second cooled product stream 79 can be 72 ℃ to 80 ℃ and all ranges and values therebetween, including 72 ℃ to 73 ℃, 73 ℃ to 74 ℃, 74 ℃ to 75 ℃, 75 ℃ to 76 ℃, 76 ℃ to 77 ℃, 77 ℃ to 78 ℃, 78 ℃ to 79 ℃, and 79 ℃ to 80 ℃. According to the present invention, the cooler 52 comprises an air cooler.
According to an embodiment of the invention, the outlet of the cooler 52 is in fluid communication with the inlet of the first gas-liquid separator 53 such that the second cooled product stream 79 flows from the cooler 52 to the first gas-liquid separator 53. The first gas-liquid separator 53 can be configured to separate the second cooled product stream 79 into a first vapor stream 80 and a liquid crude methanol stream 85. In an embodiment of the invention, the first gas-liquid separator 53 is a high pressure gas-liquid separator. The high pressure gas-liquid separator may be operated at a pressure of 80 to 95bar and all ranges and values therebetween, including 80 to 81bar, 81 to 82bar, 82 to 83bar, 83 to 84bar, 84 to 85bar, 85 to 86bar, 86 to 87bar, 87 to 88bar, 88 to 89bar, 89 to 90bar, 90 to 91bar, 91 to 92bar, 92 to 93bar, 93 to 94bar, and 94 to 95 bar. First vapor stream 80 can include unreacted carbon monoxide, unreacted hydrogen, unreacted carbon dioxide, nitrogen, methane, and uncondensed methanol. The liquid crude methanol stream 85 may include methanol, water, and paraffin wax. In an embodiment of the invention, the liquid crude methanol stream 85 comprises about 67% to 75% of the methanol from the second cooled product stream 79. The liquid crude methanol stream 85 may flow through a pressure reducing valve57 configured to reduce the pressure of the liquid crude methanol stream 85 to produce a low pressure crude methanol stream 86. In embodiments of the invention, the pressure of the low pressure crude methanol stream 86 may be from 3kg/cm to 5kg/cm and all ranges and values therebetween, including 3kg/cm2To 3.2kg/cm2、3.2kg/cm2To 3.4kg/cm2、3.4kg/cm2To 3.6kg/cm2、3.6kg/cm2To 3.8kg/cm2、3.8kg/cm2To 4.0kg/cm2、4.0kg/cm2To 4.2kg/cm2、4.2kg/cm2To 4.4kg/cm2、4.4kg/cm2To 4.6kg/cm2、4.6kg/cm2To 4.8kg/cm2And 4.8kg/cm2To 5.0kg/cm2。
In an embodiment of the invention, the outlet of pressure reducing valve 57 is in fluid communication with dewaxing unit 101 such that low pressure crude methanol stream 86 flows from pressure reducing valve 57 to dewaxing unit 101. According to an embodiment of the invention, dewaxing unit 101 is configured to remove paraffins from low pressure crude methanol stream 86 to produce wax-free methanol stream 88. In an embodiment of the invention, wax-free methanol stream 88 contains a negligible amount of paraffin wax.
According to an embodiment of the present invention, dewaxing unit 101 includes one or more cooling units arranged in parallel with each other. Dewaxing apparatus 101 can include a feed port 93 in fluid communication with one or more cooling devices. In embodiments of the present invention, fluid communication is controlled by one or more valves between the feed port 93 and the one or more cooling devices and/or in fluid communication with the feed port 93 and the one or more cooling devices. In an embodiment of the present invention, dewaxing unit 101 includes a first cooling unit 61 and a second cooling unit 60 disposed in parallel with each other, as shown in fig. 1A. The first cooling device 61 and the second cooling device 60 may be configured to remove paraffins from the low pressure crude methanol stream 86 to produce a final unfiltered methanol stream 87. In the embodiment of the present invention, only 1 of the first cooling device 61 and the second cooling device 60 is on-line in normal operation.
According to an embodiment of the present invention, when the first cooling device 61 is on-line, both valves 59 and 63 are open, the second cooling device 60 is in an idle (off-line) state, and both valves 58 and 62 are closed. When the second cooling device 60 is on-line, the first cooling device 61 is idle (off-line) and both valves 59 and 63 are closed. In an embodiment of the present invention, as the low pressure crude methanol stream 86 cools, the paraffins of the low pressure crude methanol stream 86 are deposited in the first cooling device 61. In the embodiment of the present invention, when the first cooling means 61 is deteriorated by increased wax deposition, the low pressure crude methanol stream 86 enters the second cooling means 60 and the valves 58 and 62 are opened to ensure continuous operation thereof. Meanwhile, the first cooling device 61 is taken off-line and washed with an organic solvent to remove wax deposits therein. Exemplary organic solvents may include aromatic solvents (e.g., ortho-xylene), diesel range hydrocarbons (e.g., hexadecane), cycloalkanes (e.g., cyclohexane, cyclooctane), and combinations thereof.
In an embodiment of the present invention, dewaxing apparatus 101 also includes one or more filters positioned in parallel with each other and configured to remove any traces of paraffin that may be present from final unfiltered methanol stream 87, thereby forming a wax-free methanol stream 88. According to an embodiment of the present invention, when the final unfiltered methanol stream 87 contains paraffins, the one or more filters are configured to filter the paraffins in the final unfiltered methanol stream 87. In embodiments of the invention, the one or more filters may include a first hydrophobic filter 67 and a second hydrophobic filter 66 in fluid communication with the filter feed. Fluid communication may be controlled by one or more valves (e.g., valves 65 and 69) between and/or in fluid communication with the filter feed and the first hydrophobic filter 67, and/or by one or more valves (e.g., valves 64 and 68) between and/or in fluid communication with the filter feed and the second hydrophobic filter 66. In an embodiment of the present invention, the first hydrophobic filter 67 and the second hydrophobic filter 66 may be disposed in parallel. Only one of the first and second hydrophobic filters 67 and 66 is on-line, and the other is in a standby state. When the first cooling device 67 is on-line, valves 65 and 69 are both open, the second cooling device 66 is idle (off-line), and valves 64 and 68 are both closed. When the second hydrophobic filter 66 is on-line, both valves 64 and 68 are open, the first hydrophobic filter 67 is idle (off-line) and both valves 65 and 69 are closed.
According to an embodiment of the present invention, as shown in fig. 2, dewaxing unit 101 includes a dewaxing heat exchanger 10. The dewaxing heat exchanger 10 can be horizontal or vertical. In an embodiment of the invention, the dewaxing heat exchanger 10 comprises a housing separated by a metal sheet 11, forming a first chamber 12 and a second chamber 13. The dewaxing heat exchanger 10 can include a plurality of first tube bundles 15 disposed in the first chamber 12 and a plurality of second tube bundles 14 disposed in the second chamber 13. In an embodiment of the present invention, first tube bundle 15 may be in fluid communication with second tube bundle 14 via valves 16 and 17. In embodiments of the invention, each of the first chamber 12 and the second chamber 13 may comprise 1, 3, or 5 tube passes. According to an embodiment of the present invention, the dewaxing heat exchanger 10 is configured to have a residence time sufficient to condense substantially all of the paraffin wax in the low pressure crude methanol stream 86 in the tubes of the first chamber 12 and/or the second chamber 13. According to an embodiment of the invention, each of the first chamber 12 and the second chamber 13 has separate inlets and outlets for the condensing medium, the low pressure crude methanol stream 86 and the purge liquid stream.
In an embodiment of the present invention, the dewaxing heat exchanger 10 includes a first wash liquid inlet valve 18 configured to control delivery of a first wash liquid stream 31 to the first chamber 12. In an embodiment of the invention, the dewaxing heat exchanger 10 includes a second wash liquid inlet valve 19 configured to control the delivery of a second wash liquid stream 32 to the second chamber 13. According to an embodiment of the invention, the dewaxing heat exchanger 10 comprises a first condensing medium inlet valve 23 adapted to control the delivery of a first condensing medium inlet stream 33 to the first chamber 12. The dewaxing heat exchanger 10 can also include a first condensing medium outlet valve 21 adapted to control a first condensing medium outlet stream 34 to exit the first chamber 12. In an embodiment of the invention, the dewaxing heat exchanger 10 comprises a second condensing medium inlet valve 22 adapted to control the delivery of a second condensing medium inlet flow 35 to the second chamber 13. The dewaxing heat exchanger 10 can further include a second condensing medium outlet valve 20 adapted to control a second condensing medium outlet stream 36 to exit the second chamber 13.
In an embodiment of the invention, low pressure crude methanol stream 86 may enter the tubes of first tube bank 15 through valve 16 and/or enter the tubes of second tube bank 14 through valve 17. The dewaxing heat exchanger 10 is configured such that the condensing medium is delivered to the first chamber 12 and/or the second chamber 13 through a first condensing medium inlet valve 23 and a second condensing medium inlet valve 22, respectively. During cleaning of the pipe of the first chamber 12 and/or the second chamber 13, a flow of cleaning liquid may enter the pipe through the first cleaning liquid inlet valve 18 and the second cleaning liquid inlet valve 19. An exemplary condensing medium may include water. Exemplary cleaning fluids may include aromatic solvents (e.g., ortho-xylene), diesel range hydrocarbons (e.g., hexadecane), napthenes (e.g., cyclohexane, cyclooctane), and combinations thereof. A first unfiltered methanol stream 37 can exit first tube bundle 15. A second unfiltered methanol stream 38 can exit second tube bank 14. A first unfiltered methanol stream 37 flows through valve 28 to form stream 41. A second unfiltered methanol stream 38 flows through valve 27 to form stream 42. Stream 41 and/or stream 42 then form the final unfiltered methanol stream 87. The dewaxing heat exchanger 10 can also include a filtration unit 29 configured to filter paraffin wax in the final unfiltered methanol stream 87 to form a wax-free methanol stream 88 when the final unfiltered methanol stream 87 contains paraffin wax. The filter device 29 may comprise two filters in parallel. In the present embodiment, the filtration unit 29 has only 1 filter on-line when the dewaxing heat exchanger 10 is in operation.
In an embodiment of the present invention, the dewaxing heat exchanger 10 can include a wax collection tank 26 in fluid communication with the outlet of the first chamber 12 such that the first waxy purge liquid stream 40 flows from the first chamber 12 to the wax collection tank 26. The wax collection tank 26 may be in fluid communication with an outlet of the second chamber 13 such that the second flow of wax-containing wash liquid 39 flows from the second chamber 13 to the wax collection tank 26. The flow of the first waxy wash liquid stream 40 may be controlled by valve 24. The flow of the second waxy wash liquid stream 39 may be controlled by valve 25. The wax collection tank 26 may be configured to collect cleaning fluid and/or paraffin wax.
According to an embodiment of the present invention, the first chamber 12 and the second chamber 13 of the dewaxing heat exchanger 10 may be operated independently. The first chamber 12 and the second chamber 13 of the dewaxing heat exchanger 10 shown in fig. 2 may be operated as a first cooling device 61 and a second cooling device 60, respectively, equivalent to the dewaxing device 101 shown in fig. 1A and 1B. In an embodiment of the invention, when the low pressure crude methanol stream 86 flows to the second chamber 13, the valve 17, the second condensing medium outlet valve 20, the second condensing medium inlet valve 22 and the valve 27 are opened and the second cleaning liquid inlet valve 19, the valve 25, the valve 16, the valve 28, the first condensing medium inlet valve 23, the first condensing medium outlet valve 21 are closed. In an embodiment of the invention, once the second chamber 13 is filled with paraffin, a low pressure crude methanol stream 86 is delivered to the first chamber 12, while the second chamber 13 is switched to a cleaning mode until it is ready to enter the next cycle.
According to an embodiment of the present invention, when the low pressure crude methanol stream 86 flows to the first chamber 12, the valve 16, the first condensing medium outlet valve 21, the first condensing medium inlet valve 23 and the valve 28 are opened, while the first cleaning liquid inlet valve 18, the valve 24, the valve 17, the valve 27, the second condensing medium inlet valve 22, the second condensing medium outlet valve 20 are closed. During the cleaning phase of the first chamber 12 or the second chamber 13, the cleaning solution inlet and cleaning solution outlet valves of the chamber being cleaned may be opened while the low pressure crude methanol stream 86 is processed in the other chamber. For example, when the low pressure crude methanol stream 86 is being processed in the first chamber 12, the second purging liquid inlet valve 19 and valve 25 of the second chamber 13 may be opened during purging. When the low pressure raw methanol stream 86 is being processed in the second chamber 13, the first rinse solution inlet valve 18 and valve 24 of the first chamber 12 may be opened during the rinse process.
According to an embodiment of the invention, as shown in fig. 1A, the second outlet of the first gas-liquid separator 53 may be in fluid communication with the gas cooler 54, allowing the first vapor stream 80 to flow from the first gas-liquid separator 53 to the gas cooler 54. Gas cooler 54 can be configured to cool first vapor stream 80 to produce cooled stream 81. In an embodiment of the present invention, the gas cooler 54 may use water as a cooling medium. The temperature of the cooling stream 81 can be 30 ℃ to 50 ℃ and all ranges and values therebetween, including 30 ℃ to 32 ℃, 32 ℃ to 34 ℃, 34 ℃ to 36 ℃, 36 ℃ to 38 ℃, 38 ℃ to 40 ℃, 40 ℃ to 42 ℃, 42 ℃ to 44 ℃, 44 ℃ to 46 ℃, 46 ℃ to 48 ℃, and 48 ℃ to 50 ℃. The cooling stream 81 may include methanol in the liquid phase, and unreacted carbon monoxide, hydrogen, carbon dioxide, nitrogen, and methane in the vapor phase. In embodiments of the invention, the outlet of the gas cooler 54 may be in fluid communication with the inlet of the second gas-liquid separator 55 such that the cooled stream 81 flows from the gas cooler 54 to the second gas-liquid separator 55.
In an embodiment of the present invention, the second gas-liquid separator 55 is a low temperature gas-liquid separator. Second vapor-liquid separator 55 is adapted to separate cooled stream 81 to produce a recycle gas stream 82 comprising primarily hydrogen, carbon dioxide, nitrogen and carbon monoxide, and an additional methanol stream 84 comprising primarily methanol. The additional methanol stream 84 may be substantially free of paraffins. In an embodiment of the invention, a portion of the recycle gas stream 82 may be purged as purge stream 91, with the balance of the recycle gas stream 82 forming the remaining recycle stream 83. The outlet of the second gas-liquid separator 55 may be in fluid communication with the recycle compressor 56 such that the remaining recycle stream 83 flows to the recycle compressor 56. Recycle compressor 56 can be configured to compress residual recycle stream 83. The compressed residual recycle stream 83 may be combined with the make-up syngas stream 74 to form the feed stream 75 for the methanol synthesis unit 50. In an embodiment of the invention, the recycle gas stream 82 is purged as purge stream 91 so as to avoid the build up of inert gas (nitrogen and methane) components in the heated feed stream 76.
According to an embodiment of the invention, the outlet of the dewaxing device 101 may be in fluid communication with the inlet of the pressure let-down tank 70, allowing a wax-free methanol stream 88 to flow from the dewaxing device 101 to the pressure let-down tank 70. The outlet of the second gas-liquid separator 55 may be in fluid communication with the inlet of the pressure let-down tank 70 via a pressure reducing valve (not shown) such that the additional methanol stream 84 flows from the second gas-liquid separator 55 to the pressure let-down tank 70. In an embodiment of the invention, the wax-free methanol stream 88 and the additional methanol stream 84 are combined to form a combined methanol stream 92. The combined methanol stream 92 flows to the pressure let-down tank 70. In an embodiment of the invention, the outlet of the pressure let-down tank 70 may be in fluid communication with a conventional separation device, such that the dewaxed product stream 89 flows from the pressure let-down tank 70 to the conventional separation device. In an embodiment of the invention, dewaxed product stream 89 is substantially the same composition as combined methanol stream 92. Conventional separation devices may be configured to separate water and/or dissolved gases from methanol. In an embodiment of the invention, the conventional separation apparatus comprises a washing apparatus and a distillation apparatus.
In accordance with an embodiment of the present invention, as shown in fig. 1B, the first gas-liquid separator 53 of the system 100 can be replaced by a scrub column 102 configured to separate the second cooled product stream 79 into the first vapor stream 80 and the liquid crude methanol stream 85 by scrubbing. In an embodiment of the invention, the scrubbing medium used in the scrubbing column may comprise methanol. The methanol used as scrubbing medium in scrubber 102 can come from pressure let-down tank 70 via first scrubbing medium stream 104 and/or from part of liquid crude methanol stream 85 via recycle crude methanol stream 103. In an embodiment of the invention, about 15% to 60% of the methanol in the pressure let-down tank 70 may be recycled for use as the scrubbing medium for the scrubber 102.
B. Process for the production and treatment of crude methanol
A process has been found to treat crude methanol produced from carbon monoxide, carbon dioxide and hydrogen. The method can avoid the loss of production time caused by cleaning a dewaxing device of a methanol production system. As shown in fig. 3, embodiments of the invention include a method 300 of producing and processing crude methanol. The method 300 may be practiced by the system 100 and/or the dewaxing heat exchanger 10 as shown in fig. 1A, 1B, and 2. In accordance with an embodiment of the present invention, as shown in block 301, method 300 includes processing a crude methanol stream, which may include product stream 77, to produce a liquid crude methanol stream 85 that includes primarily water, methanol, and paraffin simultaneously.
In embodiments of the invention, the processing in block 301 can include delivering a product stream 77 comprising paraffin to the feed effluent heat exchanger 51, and cooling the product stream 77 through the feed effluent heat exchanger 51, thereby forming a cooled crude methanol stream (e.g., the first cooled product stream 78). In an embodiment of the invention, the paraffin wax comprises C18Paraffin (C)18H38) To C60Paraffin (C)60H122). The temperature of the cooled crude methanol stream can be 120 ℃ to 135 ℃ and all ranges and values therebetween, including 120 ℃ to 121 ℃, 121 ℃ to 122 ℃, 122 ℃ to 123 ℃, 123 ℃ to 124 ℃, 124 ℃ to 125 ℃, 125 ℃ to 126 ℃, 126 ℃ to 127 ℃, 127 ℃ to 128 ℃, 128 ℃ to 129 ℃, 129 ℃ to 130 ℃, 130 ℃ to 131 ℃, 131 ℃ to 132 ℃, 132 ℃ to 133 ℃, 133 ℃ to 134 ℃, and 134 ℃ to 135 ℃. The cooled crude methanol stream may comprise about 94% to 98% by volume of vapor. The processing in block 301 can also include passing the first cooled product stream 78 to a cooler 52 or a first condenser, and condensing the first cooled product stream 78 within the cooler 52 or the first condenser to form a partially condensed stream, which can be the second cooled product stream 79. The temperature of the partially condensed stream may be 72 ℃ to 80 ℃ and all ranges and values therebetween, including 73 ℃, 74 ℃, 75 ℃, 76 ℃, 77 ℃, 78 ℃ and 79 ℃. The partially condensed stream may comprise from 86 vol% to 90 vol% vapor. The processing in block 301 can further include conveying the partially condensed stream to a first separator, which can include the first gas-liquid separator 53 or the scrub column 102, and separating the partially condensed stream by the first separator to form at least (1) a first vapor stream 80 including one or more of hydrogen, carbon monoxide, carbon dioxide, methane, water, and nitrogen, and (2) a liquid crude methanol stream 85 including primarily simultaneously water, methanol, and paraffin. Liquid crude methanol stream 85 can comprise 65% to 75% of the methanol from product stream 77 and all ranges and values therebetween, including 66%, 67%, 68%, 69%, 70%, 71%, 72%, 73%, and 74%.
In accordance with an embodiment of the invention, the method 300 includes sending the liquid crude methanol stream 85 to a dewaxing unit 101, as shown in block 302. As shown in block 303, the method 300 may further include separating the liquid crude methanol stream 85 in the dewaxing device 101 to form (1) a paraffin stream comprising primarily paraffin wax and (2) a wax-free methanol stream 88. In an embodiment of the invention, dewaxing unit 101 can be operated such that when first cooling unit 61 is separating the liquid crude methanol stream in-line, second cooling unit 60 is off-line, or vice versa. In an embodiment of the present invention, dewaxing unit 101 may be usedAir and/or water as cooling medium. The dewaxing apparatus 101 can cool a liquid crude methanol stream 85 to a temperature of 30 ℃ to 50 ℃ and all ranges and values therebetween, including 30 ℃ to 31 ℃, 31 ℃ to 32 ℃, 32 ℃ to 33 ℃, 33 ℃ to 34 ℃, 34 ℃ to 35 ℃, 35 ℃ to 36 ℃, 36 ℃ to 37 ℃, 37 ℃ to 38 ℃, 38 ℃ to 39 ℃, 39 ℃ to 40 ℃, 40 ℃ to 41 ℃, 41 ℃ to 42 ℃, 42 ℃ to 43 ℃, 43 ℃ to 44 ℃, 44 ℃ to 45 ℃, 45 ℃ to 46 ℃, 46 ℃ to 47 ℃, 47 ℃ to 48 ℃, 48 ℃ to 49 ℃ and 49 ℃ to 50 ℃. The dewaxing apparatus 101 may be operated at a liquid pressure of 2kg/cm2To 6kg/cm2And all ranges and values therebetween, including 2kg/cm2To 2.5kg/cm2、2.5kg/cm2To 3kg/cm2、3kg/cm2To 3.5kg/cm2、3.5kg/cm2To 4kg/cm2、4kg/cm2To 4.5kg/cm2、4.5kg/cm2To 5kg/cm2、5kg/cm2To 5.5kg/cm2And 5.5kg/cm2To 6kg/cm2. The wax-free methanol stream 88 may include negligible or less than 2ppm by weight paraffin wax.
According to an embodiment of the present invention, the method 300 further includes switching from operating the first cooling device 61 to operating the second cooling device 60, as shown in block 304. The operations may include performing the function of cooling the low pressure crude methanol stream 86 to remove paraffins therefrom. In an embodiment of the present invention, the switching of block 304 includes controlling valves 58, 59, 62, and 63 to ensure that the low pressure crude methanol stream 86 passes through the second cooling device 60 and not through the first cooling device 61. According to an embodiment of the invention, the method 300 further comprises purging the first cooling device 61 while the second cooling device 60 in the dewaxing device 101 is operating, as shown in block 305. In an embodiment of the present invention, the cleaning of block 305 may include using a cleaning medium including an aromatic solvent (e.g., ortho-xylene), a diesel range hydrocarbon (e.g., hexadecane), a cycloalkane (e.g., cyclohexane, cyclooctane), or a combination thereof to remove paraffin deposits in the first cooling device 61.
According to an embodiment of the invention, the method 300 further comprises sending the first vapor stream 80 to a gas cooler 54 (or second condenser), and cooling the first vapor stream 80 in the gas cooler 54 (or second condenser) to form a cooled stream 81 having a temperature of 45 ℃ or less than 45 ℃, as shown in block 306. In an embodiment of the invention, as shown in block 307, the process 300 further comprises passing the cooled stream 81 to a second gas-liquid separator 55 and separating the cooled stream by the second gas-liquid separator 55 to form at least (1) a second vapor stream comprising the recycle gas stream 82 comprising one or more of syngas and methane, and (2) an additional methanol stream 84 comprising primarily methanol. In an embodiment of the invention, the additional methanol stream 84 and the wax-free methanol stream 88 flow to the pressure let-down tank 70.
Although embodiments of the present invention are described with reference to the blocks in fig. 3, it should be understood that the operations of the present invention are not limited to the specific blocks and/or the specific order of the blocks illustrated in fig. 3. Thus, embodiments of the invention may use different blocks in a different order than that of FIG. 3 to provide the functionality described herein.
In the context of the present invention, at least the following 15 embodiments are disclosed. Embodiment 1 is a method of treating crude methanol containing paraffin. The method includes treating a crude methanol stream to produce a first liquid stream comprising primarily simultaneously water, methanol, and paraffin. The method further comprises delivering the first liquid stream to a dewaxing device, wherein the dewaxing device comprises a feed inlet and a first cooling device and a second cooling device disposed in parallel with each other, wherein the dewaxing device is configured such that the dewaxing device feed inlet is in fluid communication with either the first cooling device, the second cooling device, or both, wherein fluid communication is controlled by one or more valves between the dewaxing device feed inlet and the first cooling device and/or in fluid communication with the dewaxing device feed inlet and the first cooling device, and/or by one or more valves between the dewaxing device feed inlet and the second cooling device and/or in fluid communication with the dewaxing device feed inlet and the second cooling device. Further, the method includes separating the first liquid stream in a dewaxing device to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream. Embodiment 2 is the method of embodiment 1, wherein the dewaxing apparatus further includes a filter feed and a first hydrophobic filter and a second hydrophobic filter disposed in parallel with each otherA filter, wherein the dewaxing device is configured such that the filter feed is in fluid communication with the first hydrophobic filter, the second hydrophobic filter, or both, wherein fluid communication is controlled by one or more valves between and/or in fluid communication with the filter feed and the first hydrophobic filter, and/or by one or more valves between and/or in fluid communication with the filter feed and the second hydrophobic filter. Embodiment 3 is the method of embodiment 1 or 2, further comprising switching from operating the first cooling device to operating the second cooling device, and purging the first cooling device while the second cooling device is operating in the dewaxing device. Embodiment 4 is the method of any one of embodiments 1 to 3, wherein the methanol in the first liquid stream comprises about 65% to 75% of the methanol from the crude methanol stream. Embodiment 5 is the method of any one of embodiments 1 to 4, wherein the step of treating the crude methanol stream comprises conveying the crude methanol stream comprising paraffin wax to a heat exchanger, and cooling the crude methanol stream through the heat exchanger, thereby forming a cooled crude methanol stream. The method also includes conveying the cooled crude methanol stream to a first condenser, and cooling the cooled crude methanol stream in the first condenser to form a partially condensed stream. In addition, the process includes passing the partially condensed stream to a first separator and separating the partially condensed stream by the first separator to form at least (1) a first vapor stream comprising one or more of hydrogen, carbon monoxide, carbon dioxide, methane, water, and nitrogen; and (2) a first liquid stream comprising substantially simultaneously water, methanol and paraffin. Embodiment 6 is the method of embodiment 5, wherein the first separator comprises a gas-liquid separator and/or a wash column. Embodiment 7 is the method of embodiment 6, wherein the wash column is operated using a wash medium comprising a portion of the dewaxed crude methanol stream and/or a portion of the first liquid stream. Embodiment 8 is the method of any one of embodiments 5 to 7, further comprising conveying the first vapor stream to a second condenser, and cooling the first vapor stream in the second condenser to form a cooled first vapor stream having a temperature of 45 ℃ or less than 45 ℃. The method also includes flowing the cooled first vapor to a heat exchangerSent to a second separator through which the cooled first vapor stream is separated to form at least (1) a second vapor stream comprising one or more of syngas, nitrogen, and methane and (2) a second liquid stream comprising primarily methanol. Embodiment 9 is the method of embodiments 1 to 8, wherein the methanol in the second liquid stream comprises about 8% to 18% methanol from the crude methanol stream. Embodiment 10 is the method of any one of embodiments 5 to 9, wherein the temperature of the cooled crude methanol stream is from 120 ℃ to 135 ℃. Embodiment 11 is the method of any one of embodiments 5 to 10, wherein the cooled crude methanol stream contains 94 to 98 vol% of vapor. Embodiment 12 is the method of any one of embodiments 5 to 11, wherein the temperature of the partially condensed stream is from 72 ℃ to 80 ℃. Embodiment 13 is the method of any one of embodiments 5 to 12, wherein the partially condensed stream comprises 86 to 90 volume percent vapor. Embodiment 14 is the method of any one of embodiments 1 to 13, wherein the dewaxing unit is at 2kg/cm2g to 6kg/cm2g under liquid pressure. Embodiment 15 is the method of any one of embodiments 1 to 14, wherein the dewaxing unit uses a cooling medium comprising air and/or water.
Although embodiments of the present application and their advantages have been described in detail, it should be understood that various changes, substitutions and alterations can be made herein without departing from the embodiments as defined by the appended claims. Moreover, the scope of the present application is not intended to be limited to the particular embodiments of the process, machine, manufacture, composition of matter, means, methods and steps described in the specification. As one of ordinary skill in the art will readily appreciate from the disclosure, processes, machines, manufacture, compositions of matter, means, methods, or steps, presently existing or later to be developed that perform substantially the same function or achieve substantially the same result as the corresponding embodiments described herein may be utilized. Accordingly, the appended claims are intended to include within their scope such processes, machines, manufacture, compositions of matter, means, methods, or steps.
Claims (15)
1. A method of processing crude methanol comprising paraffin wax, the method comprising:
treating the crude methanol stream to produce a first liquid stream comprising predominantly simultaneously water, methanol and paraffin;
conveying the first liquid stream to a dewaxing apparatus, the dewaxing apparatus comprising:
a feed inlet; and
a first cooling device and a second cooling device disposed in parallel with one another, wherein the dewaxing device is configured such that the dewaxing device feed is in fluid communication with the first cooling device, the second cooling device, or both, wherein the fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing device feed and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed and the second cooling device; and
the first liquid stream is separated in a dewaxing unit to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream.
2. A method of processing crude methanol comprising paraffin wax, the method comprising:
treating the crude methanol stream to produce a first liquid stream comprising predominantly simultaneously water, methanol and paraffin;
conveying the first liquid stream to a dewaxing apparatus, the dewaxing apparatus comprising:
a feed inlet; and
a first cooling device and a second cooling device disposed in parallel with one another, wherein the dewaxing device is configured such that the dewaxing device feed is in fluid communication with the first cooling device, the second cooling device, or both, wherein the fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing device feed and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed and the second cooling device; and
separating the first liquid stream in a dewaxing unit to form (1) a paraffin stream comprising primarily paraffin and (2) a dewaxed crude methanol stream, wherein the dewaxing unit further comprises:
a filter feed port; and
a first hydrophobic filter and a second hydrophobic filter disposed in parallel with one another, wherein the dewaxing apparatus is configured such that the filter feed is in fluid communication with the first hydrophobic filter, the second hydrophobic filter, or both, wherein fluid communication is controlled by one or more valves between and/or in fluid communication with the filter feed and the first hydrophobic filter, and/or by one or more valves between and/or in fluid communication with the filter feed and the second hydrophobic filter.
3. The method of any one of claims 1 and 2, further comprising:
switching from operating the first cooling device to operating the second cooling device; and
the first cooling means is purged when the second cooling means is in operation in the dewaxing means.
4. The process of any one of claims 1 and 2, wherein the methanol in the first liquid stream comprises about 65% to 75% of the methanol from the crude methanol stream.
5. The process of any one of claims 1 and 2, wherein the step of treating the crude methanol stream comprises:
conveying a crude methanol stream comprising paraffin to a heat exchanger;
cooling the crude methanol stream through a heat exchanger to form a cooled crude methanol stream;
passing the cooled crude methanol stream to a first condenser;
cooling the cooled crude methanol stream in a first condenser to form a partially condensed stream;
passing the partially condensed stream to a first separator; and
separating the partially condensed stream by a first separator to form at least (1) a first vapor stream comprising one or more of hydrogen, carbon monoxide, carbon dioxide, methane, nitrogen, uncondensed methanol, and water; and (2) a first liquid stream comprising substantially simultaneously water, methanol and paraffin.
6. The process according to claim 5, wherein the first separator comprises a gas-liquid separator and/or a wash column.
7. The process of claim 6, wherein the scrub column is operated using a scrub medium comprising a portion of the dewaxed crude methanol stream and/or a portion of the first liquid stream.
8. The method of claim 5, further comprising:
passing the first vapor stream to a second condenser;
cooling the first vapor stream in a second condenser to form a cooled first vapor stream having a temperature of 45 ℃ or less than 45 ℃;
passing the cooled first vapor stream to a second separator; and
the cooled first vapor stream is separated by a second separator to form at least (1) a second vapor stream comprising one or more of syngas and methane and (2) a second liquid stream comprising primarily methanol.
9. The process of claim 8, wherein the methanol in the second liquid stream comprises from 8% to 18% methanol from the crude methanol stream.
10. The process of claim 5, wherein the temperature of the cooled crude methanol stream is from 120 ℃ to 135 ℃.
11. The process of claim 5, wherein the cooled crude methanol stream comprises 94 to 98 volume percent vapor.
12. The process of claim 5, wherein the temperature of the partially condensed stream is from 72 ℃ to 80 ℃.
13. The method of claim 5, wherein the partially condensed stream comprises from 86% to 90% by volume of vapor.
14. The method of claim 1, wherein the dewaxing unit is at 2kg/cm2g to 6kg/cm2g under liquid pressure.
15. The method of any of claims 1 and 2, wherein the dewaxing unit uses a cooling medium comprising air and/or water.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP191754548 | 2019-05-20 | ||
| EP17054548 | 2019-05-20 | ||
| PCT/IB2020/054742 WO2020234772A1 (en) | 2019-05-20 | 2020-05-19 | Online method for processing wax-containing crude methanol stream |
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| CN114531875A true CN114531875A (en) | 2022-05-24 |
| CN114531875B CN114531875B (en) | 2024-03-26 |
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