CN113788739B - Coal glycol rectification system and working method thereof - Google Patents
Coal glycol rectification system and working method thereof Download PDFInfo
- Publication number
- CN113788739B CN113788739B CN202111153328.3A CN202111153328A CN113788739B CN 113788739 B CN113788739 B CN 113788739B CN 202111153328 A CN202111153328 A CN 202111153328A CN 113788739 B CN113788739 B CN 113788739B
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- Prior art keywords
- hydrogenation
- tower
- ethylene glycol
- glycol
- reflux
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 226
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 title claims abstract description 44
- 239000003245 coal Substances 0.000 title claims abstract description 17
- 238000000034 method Methods 0.000 title claims abstract description 14
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 69
- 238000010992 reflux Methods 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 9
- 239000001257 hydrogen Substances 0.000 claims abstract description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000000926 separation method Methods 0.000 claims abstract description 5
- 150000002431 hydrogen Chemical class 0.000 claims abstract description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000003513 alkali Substances 0.000 claims description 13
- 238000005406 washing Methods 0.000 claims description 13
- 238000002834 transmittance Methods 0.000 claims description 9
- 238000004821 distillation Methods 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 5
- 239000000047 product Substances 0.000 description 37
- 238000004939 coking Methods 0.000 description 6
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 6
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 239000007791 liquid phase Substances 0.000 description 3
- 230000002035 prolonged effect Effects 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- 238000007259 addition reaction Methods 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002262 irrigation Effects 0.000 description 1
- 238000003973 irrigation Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920000728 polyester Polymers 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
- C07C29/88—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound
- C07C29/90—Separation; Purification; Use of additives, e.g. for stabilisation by treatment giving rise to a chemical modification of at least one compound using hydrogen only
-
- 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
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a coal glycol rectification system and a working method thereof, wherein the system comprises a glycol product tower, a reflux tank, a hydrogenation reactor and a hydrogenation separator; the inlet of the reflux tank is connected with the outlet of the ethylene glycol product tower, the outlet of the reflux tank is sequentially connected with the hydrogenation reactor and the hydrogenation separator, the outlets of the reflux tank and the hydrogenation separator are connected with the inlet of the ethylene glycol product tower, and the inlet of the hydrogenation reactor is connected with hydrogen; the ethylene glycol product column is provided with a reboiler. And (3) conveying the glycol at the outlet of the glycol product tower to a hydrogenation reactor through a reflux tank to react with hydrogen, enabling high-quality glycol generated in the hydrogenation reactor to enter a hydrogenation separator for gas-liquid separation, conveying the high-quality glycol to the glycol product tower, and finally, laterally withdrawing polyester-grade glycol. Reduces the generation of coked materials and prolongs the operation period of the rectification of the ethylene glycol produced by coal.
Description
Technical Field
The invention belongs to the field of glycol rectification, and relates to a coal glycol rectification system and a working method thereof.
Background
At present, the 'coking' of the reboiler is a problem of the rectifying tower of the coal-based and oil-based glycol factories, and a filter is designed for an inlet and outlet pipeline of a crude product separator aiming at the 'coking' of the reboiler. In order to reduce ethylene glycol polymerization coking, the ultra-temperature of the tower bottom and low-load operation of the rectifying tower should be avoided. In addition, the formaldehyde-removing resin and the anion exchange resin are adopted to adsorb the ethylene glycol product extracted from the rectifying side line of the coal ethylene glycol, and the two types of resin adsorption towers are operated in series, so that the problem that the formaldehyde content and the ultraviolet light transmittance of the ethylene glycol extracted from the side line exceed the standard due to the working conditions of start-stop and abnormal conditions is solved, and the times of tower washing are further reduced. However, by adopting the measures of adding a filter and resin adsorption on a pipeline, the product quality stability is poor, and the problem of coking of a reboiler at the bottom of the rectifying tower cannot be fundamentally solved.
The main reason for rectifying and coking the ethylene glycol from coal is as follows: the temperature of the tower bottom of the dealcoholization tower is 145-155 ℃, the temperature of the tower bottom of the glycol product tower is 140-150 ℃, obvious polymerization reaction can be carried out on glycol at the temperature of more than 140 ℃, the generated diethylene glycol and triethylene glycol have high viscosity, and the diethylene glycol and triethylene glycol and catalyst dust particles entering the system are polymerized into blocks as condensation cores, so that the reboiler is coked.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, and provides a coal glycol rectification system and a working method thereof, which reduce the generation of coked materials and prolong the operation period of the coal glycol rectification.
In order to achieve the purpose, the invention is realized by adopting the following technical scheme:
a coal glycol rectifying system comprises a glycol product tower, a reflux tank, a hydrogenation reactor and a hydrogenation separator;
the inlet of the reflux tank is connected with the outlet of the ethylene glycol product tower, the outlet of the reflux tank is sequentially connected with the hydrogenation reactor and the hydrogenation separator, the outlets of the reflux tank and the hydrogenation separator are connected with the reflux of the ethylene glycol product tower, and the inlet of the hydrogenation reactor is connected with hydrogen; the ethylene glycol product column is provided with a reboiler.
Preferably, the inlet of the reflux drum is connected with desalted water.
Further, the inlet of the reflux drum is connected with NaOH.
Further, a hydrogenation buffer tank is arranged between the reflux tank and the hydrogenation reactor.
Further, a hydrogenation conveying pump is arranged between the hydrogenation buffer tank and the hydrogenation reactor.
Further, a hydrogenation product pump is arranged between the hydrogenation separator and the glycol product tower.
Further, the reflux drum outlet is provided with a reflux pump.
Further, a tower kettle pump is arranged at the outlet of the glycol product tower.
The working method of the coal glycol rectification system based on any one of the above steps comprises the following steps:
when the ethylene glycol rectifying system is in normal operation, ethylene glycol in a reflux tank of an ethylene glycol product tower is pumped to a hydrogenation reactor through a reflux pump to react with hydrogen, high-quality ethylene glycol generated in the hydrogenation reactor enters a hydrogenation separator to carry out gas-liquid separation, and is sent to an ethylene glycol product tower, and finally polyester-grade ethylene glycol is extracted from a side line.
Further, after the glycol rectifying system stops running, 4% NaOH solution is added into a reflux tank, alkali liquor is sent to a tower kettle through the reflux tank, a 60-70% liquid level is established in the tower kettle of a glycol product tower, steam is added into a reboiler for boiling the tower, and alkali washing is carried out on the glycol product tower until the color of the tower kettle liquid is no longer deepened. And (3) desalted water is injected into the reflux tank, alkali washing liquid and saponified matters after alkali washing are washed through the desalted water, the pH value of the desalted water discharged by the tower kettle pump is less than 8, the ultraviolet light transmittance of the tower kettle is 275nm or more than 92%, 350nm or more than 99%, and the cleaning of the tower kettle cokes is completed.
Compared with the prior art, the invention has the following beneficial effects:
according to the invention, industrial grade ethylene glycol extracted from the top of an ethylene glycol product tower refers to a liquid phase hydrogenation technology, and under the action of a Ni catalyst, the industrial grade ethylene glycol causes a trace amount of unsaturated bonds-C=C-, -C=O, -C=C-C=O and H2 which are absorbed by ultraviolet to undergo an addition reaction, and is converted into saturated bonds which are not absorbed by ultraviolet, so that after the ultraviolet transmittance of the product is improved, materials are returned to a system, the superior product rate of the ethylene glycol can be improved from 90% to nearly 100%, and the running period of the system is prolonged.
Furthermore, the reflux tank is used for adding alkali to boil the tower, so that the cokes on the reboiler can be thoroughly cleaned.
Further, the alkaline washing liquid and the saponified product in the column can be thoroughly washed by washing the reflux drum with desalted water.
Drawings
FIG. 1 is a schematic diagram of a system according to the present invention.
Wherein: a 1-glycol product column; 2-reboiler; a 3-hydrogenation reactor; 4-hydrogenation buffer irrigation; 5-a hydrogenation separation tank; 6-a reflux drum; 7-a reflux pump; 8-a hydrogenation conveying pump; 9-a hydrogenation mixer; 10-a hydrogenation product pump; 11-tower kettle pump.
Detailed Description
The invention is described in further detail below with reference to the attached drawing figures:
as shown in fig. 1, the coal-to-ethylene glycol rectification system comprises an ethylene glycol product tower 1, a reboiler 2, a tower kettle pump 11, a reflux tank 6, a hydrogenation reactor 3, a hydrogenation buffer tank 4, a hydrogenation delivery pump 8, a hydrogenation separator 5, a hydrogenation product pump 10, a hydrogenation mixer 9 and a reflux pump 7.
The glycol product tower 1 is provided with a reboiler 2, and the outlet of the glycol product tower 1 is connected with the inlet of the reflux tank 6 and the tower kettle pump 11.
The outlet of the reflux tank 6 is sequentially connected with a reflux pump 7, a hydrogenation buffer tank 4, a hydrogenation delivery pump 8, a hydrogenation reactor 3, a hydrogenation separator 5 and a hydrogenation product pump 10, and the hydrogenation product pump 10 and the outlet pipeline of the reflux tank 6 are converged and connected with the inlet of the glycol product tower 1.
The inlet of the reflux tank 6 is connected with desalted water and NaOH.
The inlet of the hydrogenation reactor 3 is connected with hydrogen. A hydrogenation mixer 9 is arranged between the hydrogen and the hydrogenation reactor 3.
When the ethylene glycol rectifying system is in normal operation, industrial grade ethylene glycol extracted from the top of an ethylene glycol product tower 1 is sent to a liquid phase hydrogenation system through a reflux pump 7, is buffered by a hydrogenation buffer tank 4, enters a hydrogenation reactor 3 to react with fresh hydrogen, and is hydrogenated to become saturated bonds through unsaturated bonds absorbing ultraviolet, high-quality ethylene glycol generated by the reaction enters a hydrogenation separator 5 to carry out gas-liquid separation, is sent to the ethylene glycol product tower 1 through a hydrogenation product pump 10, and finally is subjected to side line extraction to obtain polyester grade ethylene glycol. The stability of the tower kettle temperature of the ethylene glycol product tower 1 is effectively controlled, and the coking of a tower kettle reboiler is reduced.
After the operation of the glycol rectifying device is stopped, 4% NaOH solution is injected into a reflux tank 6, a 60-70% liquid level is established for a glycol product tower 1 through a reflux pump 7, a tower kettle reboiler 2 is added with steam to boil the tower, alkali washing is carried out on the glycol product tower 1, the color of discharged liquid of the tower kettle pump 11 is not deepened any more, desalted water is injected into the reflux tank 6, alkali washing liquid and saponified matters after alkali washing are washed through desalted water, the pH value of the desalted water discharged by the tower kettle pump 11 is less than 8, the ultraviolet transmittance of the tower kettle is 275nm or more than 92%, 350nm or more than 99%, and the washing of the coked matters of the tower kettle is completed. Thereby prolonging the running period of the distillation of the glycol from the coal.
According to the rectification tower alkaline washing scheme, the alkaline adding flow is controlled through the concentration of alkaline solution in the reflux of the ethylene glycol product tower 1, and the concentration of alkaline solution in the reflux of the ethylene glycol product tower 1 is controlled: 3 to 4 percent. The flow rate of desalted water is controlled by the ultraviolet light transmittance of the tower bottom liquid, and the ultraviolet light transmittance of the tower bottom liquid is controlled to be 275nm or more than 92% and 350nm or more than 99%.
Industrial grade ethylene glycol extracted from the top of an ethylene glycol product tower 1 refers to a liquid phase hydrogenation technology, and under the action of a Ni catalyst, the industrial grade ethylene glycol causes a trace amount of unsaturated bonds-C=C-, -C=O, -C=C-C=O which are absorbed by ultraviolet to undergo an addition reaction with H2, and is converted into saturated bonds which are not absorbed by ultraviolet, so that after the ultraviolet transmittance of the product is improved, materials are returned to a system, the superior quality of the ethylene glycol can be improved from 90% to nearly 100%, and the running period of the system is prolonged. During the shutdown overhaul, the coke on the reboiler is thoroughly cleaned by adopting an alkaline cleaning method.
On the one hand, industrial grade glycol is hydrotreated, so that the generation of coked materials is reduced, and the operation period of distillation of coal glycol is prolonged. On the other hand, the tower is washed by adding alkali and desalted water into the reflux tank, and the packing and the reboiler tube array are thoroughly washed.
The above is only for illustrating the technical idea of the present invention, and the protection scope of the present invention is not limited by this, and any modification made on the basis of the technical scheme according to the technical idea of the present invention falls within the protection scope of the claims of the present invention.
Claims (7)
1. The working method of the coal glycol rectification system is characterized by comprising the following steps of:
when the ethylene glycol rectifying system is in normal operation, ethylene glycol at the outlet of an ethylene glycol product tower (1) is sent to a hydrogenation reactor (3) through a reflux tank (6) to react with hydrogen, high-quality ethylene glycol generated in the hydrogenation reactor (3) enters a hydrogenation separator (5) to carry out gas-liquid separation, and is sent to the ethylene glycol product tower (1) to finally obtain polyester-grade ethylene glycol in a side line;
after the glycol rectifying system stops running, desalted water is injected into the reflux tank (6), the tower wall and the filler of the glycol product tower (1) are washed through the reflux tank (6), after desalted water discharged by the tower kettle pump (11) is clean and clear, 60-70% of liquid level is established in the tower kettle of the glycol product tower (1), steam is added into the reboiler (2) to boil the tower, naOH is added into the reflux tank (6) after ultraviolet light transmittance of desalted water discharged by the tower kettle is more than or equal to 99%, alkali liquor is conveyed to the tower kettle through the reflux tank (6), alkali washing is carried out on the glycol product tower (1), and alkali washing is qualified after ultraviolet light transmittance of alkali liquor discharged by the tower kettle is more than or equal to 99%.
2. The method for operating a coal-to-ethylene glycol distillation system according to claim 1, comprising an ethylene glycol product column (1), a reflux drum (6), a hydrogenation reactor (3) and a hydrogenation separator (5);
the inlet of the reflux tank (6) is connected with the outlet of the glycol product tower (1), the outlet of the reflux tank (6) is sequentially connected with the hydrogenation reactor (3) and the hydrogenation separator (5), the outlets of the reflux tank (6) and the hydrogenation separator (5) are connected with the inlet of the glycol product tower (1), and the inlet of the hydrogenation reactor (3) is connected with hydrogen; the ethylene glycol product tower (1) is provided with a reboiler (2);
the inlet of the reflux tank (6) is connected with desalted water;
a hydrogenation buffer tank (4) is arranged between the reflux tank (6) and the hydrogenation reactor (3).
3. The method according to claim 2, wherein NaOH is connected to the inlet of the reflux drum (6).
4. The working method of the coal-to-ethylene glycol rectifying system according to claim 2, characterized in that a hydrogenation transfer pump (8) is arranged between the hydrogenation buffer tank (4) and the hydrogenation reactor (3).
5. The method according to claim 2, characterized in that a hydrogenation product pump (10) is arranged between the hydrogenation separator (5) and the ethylene glycol product column (1).
6. The method for operating a glycol rectification system from coal as claimed in claim 2, characterized in that the outlet of the reflux drum (6) is provided with a reflux pump (7).
7. The method for operating a glycol rectification system from coal as claimed in claim 2, wherein the outlet of the glycol product column (1) is provided with a column bottom pump (11).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111153328.3A CN113788739B (en) | 2021-09-29 | 2021-09-29 | Coal glycol rectification system and working method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111153328.3A CN113788739B (en) | 2021-09-29 | 2021-09-29 | Coal glycol rectification system and working method thereof |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113788739A CN113788739A (en) | 2021-12-14 |
| CN113788739B true CN113788739B (en) | 2023-12-22 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111153328.3A Active CN113788739B (en) | 2021-09-29 | 2021-09-29 | Coal glycol rectification system and working method thereof |
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Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112110794A (en) * | 2020-09-04 | 2020-12-22 | 中盐安徽红四方股份有限公司 | Production method of polyester-grade ethylene glycol |
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- 2021-09-29 CN CN202111153328.3A patent/CN113788739B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112110794A (en) * | 2020-09-04 | 2020-12-22 | 中盐安徽红四方股份有限公司 | Production method of polyester-grade ethylene glycol |
Non-Patent Citations (1)
| Title |
|---|
| 液相加氢提高聚酯级煤制乙二醇收率的工业化应用;孔会娜等;现代化工;第40卷(第8期);第200-203页 * |
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| CN113788739A (en) | 2021-12-14 |
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