CN114531875B - On-line process for treating waxy crude methanol stream - Google Patents
On-line process for treating waxy crude methanol stream Download PDFInfo
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- CN114531875B CN114531875B CN202080050739.7A CN202080050739A CN114531875B CN 114531875 B CN114531875 B CN 114531875B CN 202080050739 A CN202080050739 A CN 202080050739A CN 114531875 B CN114531875 B CN 114531875B
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 597
- 238000000034 method Methods 0.000 title claims abstract description 100
- 230000008569 process Effects 0.000 title claims description 28
- 238000001816 cooling Methods 0.000 claims abstract description 107
- 239000007788 liquid Substances 0.000 claims abstract description 82
- 239000012188 paraffin wax Substances 0.000 claims abstract description 62
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 28
- 239000007789 gas Substances 0.000 claims abstract description 24
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 15
- 238000003786 synthesis reaction Methods 0.000 claims abstract description 15
- 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
- 239000012530 fluid Substances 0.000 claims description 57
- 238000004891 communication Methods 0.000 claims description 52
- 230000002209 hydrophobic effect Effects 0.000 claims description 31
- 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 21
- 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
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 description 24
- 239000000047 product Substances 0.000 description 23
- 238000010926 purge Methods 0.000 description 19
- 238000004140 cleaning Methods 0.000 description 15
- 150000002431 hydrogen Chemical class 0.000 description 8
- 239000001993 wax Substances 0.000 description 8
- 238000005201 scrubbing Methods 0.000 description 7
- 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
- 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
- 229940078552 o-xylene Drugs 0.000 description 3
- 238000012545 processing Methods 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
- 230000008021 deposition Effects 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
- 238000012546 transfer Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000003225 biodiesel Substances 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000006184 cosolvent Substances 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
- 230000009467 reduction Effects 0.000 description 1
- 239000000126 substance 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
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Systems and methods for treating crude methanol are disclosed. A crude methanol stream comprising methanol and paraffin 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 paraffin. The dewaxing unit comprises 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 purged off-line.
Description
Of related applicationCross reference
The present application claims priority from U.S. provisional patent application No. 19175454.8 filed 5/20/2019, the entire contents of which are incorporated herein by reference.
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 using parallel cooling devices to remove paraffin wax produced as a by-product in a methanol production plant.
Background
Methanol is a colorless flammable solution that can be used in many chemical manufacturing processes and industrial settings. Methanol can be used as a raw material for producing formaldehyde which is widely used for producing polymers. Methanol can also produce olefins and gasoline through various catalytic processes. Methanol can also produce biodiesel by transesterification with glycerol. In addition, methanol is used as a cosolvent mixed in gasoline or directly as a fuel.
Currently, the most widely used method in methanol production involves a catalytic reaction between carbon monoxide, carbon dioxide and hydrogen. In this process, byproducts including paraffin wax are produced and mixed with methanol. The paraffin is then removed by a cooler. During cooling, paraffin wax may deposit in the tubes of the cooler, resulting in a decrease in the heat transfer coefficient and overall cooling capacity of the cooler. As paraffin deposits become thicker and thus the capacity for methanol production is not sustainable, the methanol production system has to be shut down for the cooler 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 remains a need for improvement in this field in view of at least the above-mentioned drawbacks of these methods.
Disclosure of Invention
Solutions have been found to address the problems described above in connection with processes for the production of methanol using synthesis gas (hydrogen, carbon monoxide and carbon dioxide). The solution consists in a method for treating crude methanol produced using synthesis gas. The process includes cooling the crude methanol stream to produce a liquid stream comprising crude methanol and paraffin, 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 device individually so that when one cooling device is cleaned off-line, the other cooling device can be operated to maintain operation of the overall methanol production system. Thus, the method can prevent the complete shutdown of the methanol production system due to the need to purge the cooling device of the paraffin wax accumulated. Thus, the process may reduce or eliminate the loss of production time suffered by conventional methanol production systems and processes. The process of the present invention thus provides a technical solution to at least some of the problems associated with the conventional systems and processes for producing methanol described above.
Embodiments of the invention include a method of treating crude methanol comprising paraffin wax. The method includes treating a crude methanol stream to produce a first liquid stream that includes primarily water, methanol, and paraffin simultaneously. The method further includes delivering the first liquid stream to a dewaxing apparatus. The dewaxing device comprises (a) a feeding hole and (b) a first cooling device and a second cooling device which are mutually connected in parallel. The dewaxing unit is configured such that the dewaxing unit feed is in fluid communication with the first cooling unit, the second cooling unit, 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 cooling unit and/or by one or more valves between and/or in fluid communication with the dewaxing unit feed and the second cooling unit. The process further includes separating the first liquid stream in a dewaxing unit to form (1) a paraffin stream comprising predominantly paraffin and (2) a dewaxed raw methanol stream.
Embodiments of the invention include a method of treating crude methanol comprising paraffin wax. The method includes treating a crude methanol stream to produce a first liquid stream that includes primarily water, methanol, and paraffin simultaneously. The dewaxing device comprises a dewaxing device feed inlet. The dewaxing device further comprises a first cooling device and a second cooling device which are mutually connected in parallel. The dewaxing unit is configured such that the dewaxing unit feed is in fluid communication with the first cooling unit, the second cooling unit, 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 cooling unit and/or by one or more valves between and/or in fluid communication with the dewaxing unit feed and the second cooling unit. The dewaxing device also comprises (1) a filter feed inlet and (2) a first hydrophobic filter and a second hydrophobic filter which are mutually connected in parallel. 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. 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 further includes separating the first liquid stream in a dewaxing unit to form (1) a paraffin stream comprising predominantly paraffin and (2) a dewaxed raw methanol stream.
Embodiments of the invention include a method of treating crude methanol comprising paraffin wax. The process includes passing a crude methanol stream comprising paraffin to a heat exchanger. The method further 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% to 98% by volume vapor. The method further includes delivering the cooled crude methanol stream to a first condenser. The method further includes cooling the cooled crude methanol stream in a first condenser to form a partially condensed stream having a temperature of 72 ℃ to 80 ℃ and/or comprising 86% to 90% by volume vapor. The method further includes passing the partially condensed stream to a first separator. The method 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 primarily water, methanol, and paraffin simultaneously. The method further includes delivering the first vapor stream to a second condenser. The method further 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 method further includes delivering the cooled first vapor stream to a second separator. The method further includes separating the cooled first vapor stream via a second separator to form at least (1) a second vapor stream comprising one or more of synthesis gas, nitrogen, and methane and (2) a second liquid stream comprising primarily methanol. The method further includes delivering the first liquid stream to a dewaxing apparatus. The dewaxing device comprises a dewaxing device feed inlet. The method further comprises a first cooling device and a second cooling device arranged in parallel with each other. The dewaxing unit is configured such that the dewaxing unit feed is in fluid communication with the first cooling unit, the second cooling unit, 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 cooling unit and/or by one or more valves between and/or in fluid communication with the dewaxing unit feed and the second cooling unit. The dewaxing apparatus further includes a filter feed. The dewaxing apparatus further includes a first hydrophobic filter and a second hydrophobic filter disposed in parallel with each other. 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. The fluid communication is controlled by one or more valves between and/or in fluid communication with the filter feed inlet and the first hydrophobic filter and/or by one or more valves between and/or in fluid communication with the filter feed inlet and the second hydrophobic filter. The process further includes separating the first liquid stream in a dewaxing unit to form (1) a paraffin stream comprising predominantly paraffin and (2) a dewaxed raw methanol stream comprising predominantly methanol.
The following includes definitions of various terms and phrases used throughout this specification.
The terms "about" or "approximately" are defined as being in close proximity as understood by one of ordinary skill in the art. In one non-limiting embodiment, the term is defined as a range comprised within 10%, preferably within 5%, more preferably within 1%, most preferably within 0.5%.
The terms "wt%", "volume%" or "mole%" refer to the percentage of the weight, volume or number of moles of a component in the total weight, total volume or total number of moles of the material comprising the component, respectively. In one non-limiting embodiment, 10 mole of the component in 100 mole of the material is 10 mole% of the component.
The term "substantially" and variants thereof are defined as including ranges within 10%, within 5%, within 1%, or within 0.5%.
The term "inhibit" or "reduce" or "prevent" or "avoid" or any variant of these terms when used in the claims and/or specification includes any measurable reduction or complete inhibition in order to achieve the intended result.
The term "effective" when used in the claims and/or specification means sufficient to achieve a desired, expected, or intended result.
When used in a claim or specification with "comprising," including, "" containing, "or" having, "the use of a numerical designation in front of elements may mean" one "but it also corresponds to the meaning of" 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 can be "comprised," consisting essentially of, "or" consist of the specific materials, ingredients, compositions, etc., disclosed throughout this specification.
The term "predominantly" when used in the claims and/or specification refers to any of greater than 50 wt%, 50 mole% and 50 volume%. For example, "predominantly" may include 50.1 to 100 wt% and all ranges and values therebetween, 50.1 to 100 mole% and all ranges and values therebetween, or 50.1 to 100 volume% and all ranges and values therebetween.
Other objects, features and advantages of the present invention will become apparent from the following drawings, detailed description and examples. It should be understood, however, that the drawings, detailed description and examples, while indicating specific embodiments of the invention, are given by way of illustration only and not by way of limitation. It is further contemplated that variations, combinations, and modifications within the spirit and scope of the invention will be apparent to those skilled in the art from this detailed description. In other implementations, features from a particular embodiment may be combined with features from other embodiments. For example, features from one embodiment may be combined with features from any other embodiment. 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 an effluent of a methanol synthesis unit, according to an embodiment of the invention;
FIG. 1B shows a schematic diagram of a system for producing methanol including a methanol scrubber for separating the effluent of a methanol synthesis unit, according to an embodiment of the invention;
FIG. 2 shows a schematic diagram of a dewaxing heat exchanger of a dewaxing apparatus according to an embodiment of the 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 crude methanol produced, including by-product paraffins, is then condensed in a series of cooling units to remove the paraffins and purify the methanol. However, as paraffin gradually deposits 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 dewaxed raw methanol cannot meet the production requirements. Typically, to clean the cooling unit, the entire methanol production system must be shut down, resulting in a loss of production time and run time of the production system. The present invention provides a solution to at least the problem. The solution is premised on a method of treating crude methanol, comprising cooling the crude methanol produced using synthesis gas by means of two or more cooling devices arranged in parallel with each other, such that when one of the cooling devices is taken off-line, e.g. cleaned, the system can be maintained in operation by using the other cooling devices in the system. Accordingly, the total production time and the running time of the methanol production system can be improved as compared with the conventional method, and the productivity of methanol can be improved as compared with the conventional method. This and other non-limiting aspects of the 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 than one gas-liquid separators. Referring to fig. 1A, a schematic diagram of a system 100 that is capable of continuous methanol production without stopping the system due to paraffin build-up in the dewaxing unit can be seen. In accordance with an embodiment of the invention, the system 100 may include a methanol synthesis unit 50 that may react 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 byproducts (e.g., ethanol); unreacted synthesis gas, including carbon monoxide, carbon dioxide, hydrogen, methane and inert gases (such as nitrogen); or a combination thereof. The paraffin wax may comprise C 18 Paraffin (C) 18 H 38 ) To C 60 Paraffin (C) 60 H 122 ). In an embodiment of the present invention, the methanol synthesis unit 50 includes a catalyst comprising CuO, znO, al 2 O 3 Or a combination thereof. In embodiments of the present 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% DEG C, 171 DEG to 172 ℃, 172 DEG to 173 ℃, 173 DEG to 174 ℃, 174 DEG to 175 ℃, 175 DEG to 176 ℃, 176 DEG to 177 ℃, 177 DEG to 178 ℃, 178 DEG to 179 ℃ and 179 DEG to 180 ℃. The temperature of 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/cm 2 To 110kg/cm 2 And all ranges and values therebetween, including 80kg/cm 2 To 82kg/cm 2 、82kg/cm 2 To 84kg/cm 2 、84kg/cm 2 To 86kg/cm 2 、86kg/cm 2 To 88kg/cm 2 、88kg/cm 2 To 90kg/cm 2 、90kg/cm 2 To 92kg/cm 2 、92kg/cm 2 To 94kg/cm 2 、94kg/cm 2 To 96kg/cm 2 、96kg/cm 2 To 98kg/cm 2 、98kg/cm 2 To 100kg/cm 2 、100kg/cm 2 To 102kg/cm 2 、102kg/cm 2 To 104kg/cm 2 、104kg/cm 2 To 106kg/cm 2 、106kg/cm 2 To 108kg/cm 2 And 108kg/cm 2 To 110kg/cm 2 。
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 present invention, the cooler 52 is configured to cool the first cooled product stream 78 to produce the 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 95bar. The 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 can include methanol, water, and paraffin. In an embodiment of the invention, the liquid crude methanol stream 85 comprises from about 67% to 75% methanol from the second cooled product stream 79. The liquid crude methanol stream 85 may flow through a pressure relief valve 57 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 3kg/cm to 5kg/cm and all ranges and values therebetween, including 3kg/cm 2 To 3.2kg/cm 2 、3.2kg/cm 2 To 3.4kg/cm 2 、3.4kg/cm 2 To 3.6kg/cm 2 、3.6kg/cm 2 To 3.8kg/cm 2 、3.8kg/cm 2 To 4.0kg/cm 2 、4.0kg/cm 2 To 4.2kg/cm 2 、4.2kg/cm 2 To 4.4kg/cm 2 、4.4kg/cm 2 To 4.6kg/cm 2 、4.6kg/cm 2 To 4.8kg/cm 2 And 4.8kg/cm 2 To 5.0kg/cm 2 。
In an embodiment of the invention, the outlet of the pressure relief valve 57 is in fluid communication with the dewaxing apparatus 101 such that the low pressure raw methanol stream 86 flows from the pressure relief valve 57 to the dewaxing apparatus 101. Dewaxing apparatus 101 is configured to remove paraffin from low pressure crude methanol stream 86 to produce a wax-free methanol stream 88 in accordance with an embodiment of the invention. In an embodiment of the present invention, the wax-free methanol stream 88 contains negligible amounts of paraffin.
According to an embodiment of the invention, the dewaxing unit 101 comprises one or more cooling units arranged in parallel to each other. Dewaxing apparatus 101 can include a feed 93 in fluid communication with one or more cooling apparatuses. In embodiments of the present invention, fluid communication is controlled by one or more valves between and/or in fluid communication with the feed inlet 93 and one or more cooling devices. In an embodiment of the present invention, dewaxing apparatus 101 includes a first cooling apparatus 61 and a second cooling apparatus 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 paraffin from the low pressure raw 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 are in line during 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, paraffin wax of the low pressure crude methanol stream 86 is deposited in the first cooling unit 61. In an embodiment of the present invention, when the first cooling device 61 is deteriorated by increased wax deposition, the low pressure raw methanol stream 86 enters the second cooling device 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 deposition therein. Exemplary organic solvents can include aromatic solvents (e.g., o-xylene), diesel range hydrocarbons (e.g., hexadecane), naphthenes (e.g., cyclohexane, cyclooctane), and combinations thereof.
In an embodiment of the present invention, dewaxing unit 101 further includes one or more filters disposed in parallel with each other configured to remove any wax marks that may be present from the final unfiltered methanol stream 87 to form a wax-free methanol stream 88. In accordance with an embodiment of the present invention, when the final unfiltered methanol stream 87 contains paraffin, the one or more filters are configured to filter paraffin 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 inlet. The 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 inlet 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 inlet 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 in line, and the other is in a standby state. When the first cooling means 67 is on-line, both valves 65 and 69 are open, the second cooling means 66 is idle (off-line), and both valves 64 and 68 are 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 apparatus 101 includes a dewaxing heat exchanger 10. The dewaxing heat exchanger 10 may 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 may 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 embodiments of the present invention, the first tube bundle 15 may be in fluid communication with the second tube bundle 14 through 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 invention, the dewaxing heat exchanger 10 is configured to have a residence time sufficient to condense substantially all of the paraffin in the low pressure raw 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 condensing medium, low pressure raw methanol stream 86, and purge liquid stream.
In an embodiment of the present invention, dewaxing heat exchanger 10 includes a first cleaning fluid inlet valve 18 configured to control the delivery of a first cleaning fluid stream 31 to the first chamber 12. In an embodiment of the invention, the dewaxing heat exchanger 10 comprises a second cleaning fluid inlet valve 19 configured for controlling the delivery of a second cleaning fluid 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 may also include a first condensing medium outlet valve 21 adapted to control the first condensing medium outlet stream 34 exiting 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 stream 35 to the second chamber 13. The dewaxing heat exchanger 10 may also include a second condensing medium outlet valve 20 adapted to control the second condensing medium outlet stream 36 from exiting the second chamber 13.
In embodiments of the present invention, low pressure raw methanol stream 86 may enter the tubes of first tube bundle 15 through valve 16 and/or enter the tubes of second tube bundle 14 through valve 17. The dewaxing heat exchanger 10 is configured such that condensing medium is fed to the first chamber 12 and/or the second chamber 13 via a first condensing medium inlet valve 23 and a second condensing medium inlet valve 22, respectively. During cleaning of the conduit of the first chamber 12 and/or the second chamber 13, a flow of cleaning liquid may enter the conduit 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., o-xylene), diesel range hydrocarbons (e.g., hexadecane), naphthenes (e.g., cyclohexane, cyclooctane), and combinations thereof. The first unfiltered methanol stream 37 can be discharged from the first tube bundle 15. The second unfiltered methanol stream 38 can be discharged from the second tube bundle 14. First unfiltered methanol stream 37 flows through valve 28 to form stream 41. The 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. Dewaxing heat exchanger 10 may also include a filtration device 29 configured to filter the paraffin in final unfiltered methanol stream 87 to form a wax-free methanol stream 88 when the paraffin is contained in final unfiltered methanol stream 87. The filter device 29 may comprise two filters connected in parallel. In an embodiment of the present invention, only 1 filter of the filtration unit 29 is in-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 having an outlet in fluid communication with the first chamber 12 such that a first waxy purge 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 the outlet of the second chamber 13 such that a second waxy purge stream 39 flows from the second chamber 13 to the wax collection tank 26. The flow of the first waxy purge stream 40 may be controlled by valve 24. The flow of the second waxy purge stream 39 may be controlled by valve 25. The wax collection tank 26 may be configured to collect cleaning liquid and/or paraffin.
According to an embodiment of the invention, the first chamber 12 and the second chamber 13 of the dewaxing heat exchanger 10 are independently operable. The first chamber 12 and the second chamber 13 of the dewaxing heat exchanger 10 as shown in fig. 2 are operable 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, valve 17, second condensing medium outlet valve 20, second condensing medium inlet valve 22 and valve 27 are open and second purging liquid inlet valve 19, valve 25, valve 16, valve 28, first condensing medium inlet valve 23, first condensing medium outlet valve 21 are closed when low-pressure raw methanol stream 86 flows to second chamber 13. In an embodiment of the invention, once the second chamber 13 is filled with paraffin, the low pressure crude methanol stream 86 is delivered to the first chamber 12 while the second chamber 13 is switched to the purge mode until it is ready to enter the next cycle.
According to an embodiment of the present invention, when the low pressure raw 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 purge phase of either the first chamber 12 or the second chamber 13, the purge liquid inlet and purge liquid outlet valves of the purged chamber may be opened while the low pressure raw methanol stream 86 is being processed in the other chamber. For example, the second purge liquid inlet valve 19 and valve 25 of the second chamber 13 may be opened during a purge while the low pressure raw methanol stream 86 is being processed in the first chamber 12. When the low pressure raw methanol stream 86 is being processed in the second chamber 13, the first cleaning liquid inlet valve 18 and valve 24 of the first chamber 12 may be opened during the cleaning process.
According to embodiments 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, causing a first vapor stream 80 to flow from the first gas-liquid separator 53 to the gas cooler 54. Gas cooler 54 may 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 may 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 cooling stream 81 flows from the gas cooler 54 to the second gas-liquid separator 55.
In an embodiment of the invention, the second gas-liquid separator 55 is a low temperature gas-liquid separator. The second gas-liquid separator 55 is adapted to separate a cooling 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 paraffin. In embodiments 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 remainder recycle stream 83. The outlet of the second gas-liquid separator 55 may be in fluid communication with the recycle compressor 56, with the remaining recycle stream 83 flowing to the recycle compressor 56. The recycle compressor 56 may be configured to compress the 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 present invention, the recycle gas stream 82 is purged as purge stream 91 so that the accumulation of inert gas (nitrogen and methane) components in the heated feed stream 76 is avoided.
According to embodiments of the invention, the outlet of the dewaxing apparatus 101 may be in fluid communication with the inlet of the pressure relief tank 70 such that the waxless methanol stream 88 flows from the dewaxing apparatus 101 to the pressure relief tank 70. The outlet of the second gas-liquid separator 55 may be in fluid communication with the inlet of the pressure relief tank 70 via a pressure relief valve (not shown) such that additional methanol stream 84 flows from the second gas-liquid separator 55 to the pressure relief tank 70. In an embodiment of the present 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 pressure relief tank 70. In embodiments of the present invention, the outlet of pressure relief tank 70 may be in fluid communication with a conventional separation device, allowing dewaxed product stream 89 to flow from pressure relief tank 70 to the conventional separation device. In an embodiment of the present 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 present invention, the conventional separation apparatus includes 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 with a scrubber 102 configured to separate the second cooled product stream 79 into a first vapor stream 80 and a liquid crude methanol stream 85 by scrubbing. In embodiments of the present invention, the scrubbing medium used in the scrubbing tower may comprise methanol. Methanol used as a scrubbing medium in scrubbing tower 102 can be from pressure relief tank 70 via first scrubbing medium stream 104 and/or from a portion of liquid crude methanol stream 85 via recycle crude methanol stream 103. In an embodiment of the present invention, about 15% to 60% of the methanol in the pressure relief tank 70 may be recycled as the scrubbing medium of the scrubber 102.
B. Process for producing and treating crude methanol
A process for treating crude methanol produced with carbon monoxide, carbon dioxide and hydrogen has been found. The method can avoid the loss of production time caused by cleaning the dewaxing device of the methanol production system. As shown in fig. 3, an embodiment of the invention includes a method 300 of producing and treating crude methanol. The method 300 may be practiced with 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, the method 300 includes treating a crude methanol stream, which may include the 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 may 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 C 18 Paraffin (C) 18 H 38 ) To C 60 Paraffin (C) 60 H 122 ). The temperature of the cooled crude methanol stream may 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 from about 94% to 98% by volume of vapor. The processing in block 301 may also include delivering the first cooled product stream 78 to the cooler 52 or first condenser and condensing the first cooled product stream 78 within the cooler 52 or first condenser to form a partially condensed stream, which may 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 DEG C and 79 ℃. The partially condensed stream may comprise 86% to 90% by volume of vapor. The processing in block 301 can also include passing the partially condensed stream to a first separator, which can include the first vapor-liquid separator 53 or the scrub column 102, and separating the partially condensed stream through the first separator to form at least (1) a first vapor stream 80 that includes one or more of hydrogen, carbon monoxide, carbon dioxide, methane, water, and nitrogen, and (2) a liquid crude methanol stream 85 that includes primarily water, methanol, and paraffins simultaneously. The liquid crude methanol stream 85 can include 65% to 75% and all ranges and values therebetween, including 66%, 67%, 68%, 69%, 70%, 71%, 72%, 73%, and 74% of the methanol from the product stream 77.
In accordance with an embodiment of the present invention, as shown in block 302, the method 300 includes delivering a liquid crude methanol stream 85 to a dewaxing unit 101. As shown in block 303, the method 300 may further include separating the liquid crude methanol stream 85 in the dewaxing unit 101 to form (1) a paraffin stream comprising primarily paraffin and (2) a waxy methanol stream 88. In embodiments of the invention, dewaxing unit 101 may be operated such that second cooling unit 60 is off-line, or vice versa, when first cooling unit 61 separates the liquid crude methanol stream on-line. In embodiments of the present invention, dewaxing apparatus 101 can use air and/or water as a cooling medium. Dewaxing unit 101 may cool liquid crude methanol stream 85 to a temperature of from 30 ℃ to 50 ℃ and all ranges and values therebetween, including from 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 ℃. Dewaxing apparatus 101 may be operated at a liquid pressure of 2kg/cm 2 To 6kg/cm 2 And all ranges and values therebetween, including 2kg/cm 2 To 2.5kg/cm 2 、2.5kg/cm 2 To 3kg/cm 2 、3kg/cm 2 To 3.5kg/cm 2 、3.5kg/cm 2 To 4kg/cm 2 、4kg/cm 2 To 4.5kg/cm 2 、4.5kg/cm 2 To 5kg/cm 2 、5kg/cm 2 To 5.5kg/cm 2 And 5.5kg/cm 2 To 6kg/cm 2 . The wax-free methanol stream 88 can include negligible or less than 2ppm by weight of paraffin wax.
According to an embodiment of the present invention, as shown in block 304, the method 300 further includes switching from operating the first cooling device 61 to operating the second cooling device 60. The operations may include performing the function of cooling the low pressure crude methanol stream 86 to remove paraffins therein. 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 raw methanol stream 86 passes through the second cooling device 60 and not through the first cooling device 61. In accordance with an embodiment of the present invention, as shown in block 305, the method 300 further includes purging the first cooling unit 61 while the second cooling unit 60 in the dewaxing unit 101 is operating. In embodiments of the present invention, the purging of block 305 may include using a purging medium including an aromatic solvent (e.g., o-xylene), a diesel range hydrocarbon (e.g., hexadecane), a naphthene (e.g., cyclohexane, cyclooctane), or a combination thereof to remove paraffin deposits in the first cooling unit 61.
In accordance with an embodiment of the present invention, as shown in block 306, the method 300 further includes delivering the first vapor stream 80 to the 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 ℃. In an embodiment of the invention, as shown in block 307, the method 300 further includes delivering a cooling stream 81 to the second gas-liquid separator 55 and separating the cooling 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 synthesis gas and methane, and (2) an additional methanol stream 84 comprising primarily methanol. In an embodiment of the present invention, an additional methanol stream 84 and a wax-free methanol stream 88 flow to pressure relief tank 70.
While embodiments of the invention are described in terms of blocks in fig. 3, it should be understood that the operations of the invention are not limited to the specific blocks and/or the specific order of blocks shown 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 process for treating crude methanol containing paraffin. The method includes treating a crude methanol stream to produce a first liquid stream that includes primarily water, methanol, and paraffin simultaneously. 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 arranged in parallel with each other, wherein the dewaxing device is configured such that the dewaxing device feed inlet 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 inlet and the first cooling device, and/or by one or more valves between and/or in fluid communication with the dewaxing device feed inlet and the second cooling device. Further, the process includes separating the first liquid stream in a dewaxing unit to form (1) a paraffin stream comprising predominantly paraffin and (2) a dewaxed raw methanol stream. Embodiment 2 is the method of embodiment 1, wherein the dewaxing apparatus further comprises a filter feed and a first hydrophobic filter and a second hydrophobic filter disposed in parallel with each other, 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 the 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 unit to operating the second cooling unit, and purging the first cooling unit while the second cooling unit is in operation in the dewaxing unit. Embodiment 4 is the method of any one of embodiments 1 to 3, wherein the methanol in the first liquid stream comprises from about 65% to 75% methanol from the crude methanol stream. Embodiment 5 is embodiments 1 to The method of any one of 4, wherein the step of treating the crude methanol stream comprises passing the crude methanol stream comprising paraffin to a heat exchanger and cooling the crude methanol stream through the heat exchanger to form a cooled crude methanol stream. The method further includes delivering 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. Further, the method 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 primarily water, methanol, and paraffin simultaneously. Embodiment 6 is the method of embodiment 5, wherein the first separator comprises a gas-liquid separator and/or a scrubber. Embodiment 7 is the method of embodiment 6, wherein the scrub column is operated with a scrub 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 passing 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. The method further includes passing the cooled first vapor stream to a second separator, and separating the cooled first vapor stream by the second separator to form at least (1) a second vapor stream comprising one or more of synthesis gas, 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 from 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 cooled crude methanol stream has a temperature of 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% by volume of vapor. Embodiment 12 is the method of any one of embodiments 5 to 11, wherein the temperature of the partially condensed stream is 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% by volume Is a vapor of (a). Embodiment 14 is the method of any one of embodiments 1 to 13, wherein the dewaxing apparatus is at 2kg/cm 2 g to 6kg/cm 2 g operating under liquid pressure. Embodiment 15 is the method of any one of embodiments 1 to 14, wherein the dewaxing apparatus 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. Furthermore, 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. One of ordinary skill in the art will readily appreciate from the disclosure that 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 treating crude methanol comprising paraffin wax, the method comprising:
Treating the crude methanol stream to produce a first liquid stream comprising primarily water, methanol, and paraffin simultaneously;
delivering the first liquid stream to a dewaxing apparatus comprising:
a feed inlet;
a first cooling device and a second cooling device which are mutually connected in parallel,
a filter feed inlet; and
a first hydrophobic filter and a second hydrophobic filter arranged in parallel with each other;
wherein the dewaxing unit is configured to place the dewaxing unit feed in fluid communication with the first cooling unit, the second cooling unit, or both, wherein the fluid communication is controlled by one or more valves between and/or in fluid communication with the dewaxing unit feed and the first cooling unit, and/or by one or more valves between and/or in fluid communication with the dewaxing unit feed and the second cooling unit; and separating the first liquid stream in a dewaxing unit to form a paraffin stream comprising predominantly paraffin and a dewaxed raw methanol stream.
2. The method of claim 1, wherein the dewaxing apparatus is configured to place the filter feed in fluid communication with the first hydrophobic filter, the second hydrophobic filter, or both.
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 unit is purged while the second cooling unit is operating in the dewaxing unit.
4. The process of any one of claims 1 and 2, wherein the methanol in the first liquid stream comprises from 65% to 75% methanol from the crude methanol stream.
5. The method of any one of claims 1 and 2, wherein the step of treating the crude methanol stream comprises:
passing the 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 a portion of the condensed stream to a first separator; and
separating the partially condensed stream by a first separator to form at least a first vapor stream comprising one or more of hydrogen, carbon monoxide, carbon dioxide, methane, nitrogen, uncondensed methanol, and water; and a first liquid stream comprising primarily water, methanol and paraffin simultaneously.
6. The method of claim 5, wherein the first separator comprises a gas-liquid separator and/or a scrubber.
7. The method of claim 6, wherein the scrub column is operated with 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 a second vapor stream comprising at least one or more of synthesis gas and methane and a second liquid stream comprising primarily methanol.
9. The method of claim 8, wherein the methanol in the second liquid stream comprises 8% to 18% methanol from the crude methanol stream.
10. The process of claim 5, wherein the cooled crude methanol stream has a temperature of 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 process 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 apparatus is at 2kg/cm 2 g to 6kg/cm 2 g operating under liquid pressure.
15. The method of any of claims 1 and 2, wherein the dewaxing apparatus uses a cooling medium comprising air and/or water.
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| EP17054548 | 2019-05-20 | ||
| EP191754548 | 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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| CN114531875B true CN114531875B (en) | 2024-03-26 |
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