CN113072428B - Replacement thermal coupling process for vacuum induced air for ethylene glycol rectification separation - Google Patents
Replacement thermal coupling process for vacuum induced air for ethylene glycol rectification separation Download PDFInfo
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- CN113072428B CN113072428B CN202110412168.3A CN202110412168A CN113072428B CN 113072428 B CN113072428 B CN 113072428B CN 202110412168 A CN202110412168 A CN 202110412168A CN 113072428 B CN113072428 B CN 113072428B
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- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 title claims abstract description 389
- 238000010168 coupling process Methods 0.000 title claims abstract description 145
- 238000000926 separation method Methods 0.000 title claims abstract description 13
- 230000008878 coupling Effects 0.000 claims abstract description 132
- 238000005859 coupling reaction Methods 0.000 claims abstract description 132
- 238000000034 method Methods 0.000 claims abstract description 46
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 91
- 238000010438 heat treatment Methods 0.000 claims description 83
- 238000001816 cooling Methods 0.000 claims description 59
- 238000007670 refining Methods 0.000 claims description 36
- 238000004519 manufacturing process Methods 0.000 claims description 34
- 230000018044 dehydration Effects 0.000 claims description 22
- 238000006297 dehydration reaction Methods 0.000 claims description 22
- 230000001105 regulatory effect Effects 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 16
- 230000001502 supplementing effect Effects 0.000 claims description 8
- 238000005194 fractionation Methods 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 2
- 230000000153 supplemental effect Effects 0.000 claims 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 abstract description 21
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 18
- 238000009833 condensation Methods 0.000 description 17
- 230000005494 condensation Effects 0.000 description 17
- 239000012530 fluid Substances 0.000 description 11
- MTHSVFCYNBDYFN-UHFFFAOYSA-N diethylene glycol Chemical compound OCCOCCO MTHSVFCYNBDYFN-UHFFFAOYSA-N 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000011084 recovery Methods 0.000 description 7
- MUBZPKHOEPUJKR-UHFFFAOYSA-N Oxalic acid Chemical compound OC(=O)C(O)=O MUBZPKHOEPUJKR-UHFFFAOYSA-N 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 238000004326 stimulated echo acquisition mode for imaging Methods 0.000 description 4
- 239000013589 supplement Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000013021 overheating Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 description 3
- 230000008016 vaporization Effects 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 229940083957 1,2-butanediol Drugs 0.000 description 1
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 description 1
- BMRWNKZVCUKKSR-UHFFFAOYSA-N butane-1,2-diol Chemical compound CCC(O)CO BMRWNKZVCUKKSR-UHFFFAOYSA-N 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000006482 condensation reaction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000007907 direct compression Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
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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
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F27/00—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus
- F28F27/02—Control arrangements or safety devices specially adapted for heat-exchange or heat-transfer apparatus for controlling the distribution of heat-exchange media between different channels
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a replacement thermal coupling process of vacuum induced air for ethylene glycol rectification separation, which adopts a vacuum system to guide the coupling heat exchange of dihydric alcohol steam (S1) at the top of a debutanizer and a heated stream (S5); the pressure of the dihydric alcohol steam (S1) is 0.2-0.6bar, and the dihydric alcohol steam is completely condensed by sequentially passing through a coupling heat exchanger (E-C) and a condenser (E1) which are connected in series, wherein the top position of the shell side of the condenser (E1) far away from the dihydric alcohol steam inlet is connected with a vacuum system (P1), the flow of the dihydric alcohol steam is guided by the vacuum system (P1), and the pressure of the top of the de-butanol tower is adjusted; the heated stream (S5) was split into two parts in parallel and heated by coupled heat exchangers (E-C) and heater (E2), respectively. Compared with the prior art, the method adopts the vacuum system to guide the dihydric alcohol steam at the top of the de-butanol tower to the adjacent tower to perform coupled heat exchange with the heated stream, does not need a steam conveying machine and is convenient to control and operate.
Description
Technical Field
The invention relates to the technical field of chemical production, in particular to a thermal coupling energy-saving process method in the rectification separation process of ethylene glycol.
Background
At present, a plurality of sets of industrial scale devices are operated for preparing the ethylene glycol by adopting synthesis gas, the oxalate is generated by CO oxidation coupling, and then the ethylene glycol is prepared by the hydrogenation of the oxalate. The product of the process is introduced with impurities such as lower carboxylic acid and esters thereof, propylene glycol, butanediol and the like, great difficulty is added to the rectification and separation of the ethylene glycol, and an ethylene glycol rectification and separation system at least needs a dehydration tower, an oxalate removal tower, a debutanizer and an ethylene glycol refining tower, wherein the boiling points of the ethylene glycol and the 1, 2-butanediol are close, the separation difficulty is great, and the energy consumption of the debutanizer accounts for about 40 percent of that of the ethylene glycol rectification process. The temperature of the glycol steam at the top of the de-butanol tower is higher than 150 ℃ under the common operating pressure (table 1), and the recovery and utilization of the latent heat of condensation of the steam have important significance for reducing the energy consumption of the ethylene glycol production.
TABLE 1
| Overhead pressure/bar of the de-butanol | Glycol vapor saturation temperature/° c |
| 0.2 | 150 |
| 0.24 | 155 |
| 0.29 | 160 |
| 0.35 | 165 |
| 0.42 | 170 |
| 0.50 | 175 |
Patent CN104788289A proposes to use heat pump rectification in the de-butanol tower, but has the following problems: firstly, the dihydric alcohol steam at the top of the tower can not be directly compressed, an indirect heat pump is needed, the temperature of the water vapor generated by utilizing the latent heat of the dihydric alcohol steam is lower than the temperature at the top of the tower, and the direct heat pump needs larger compression ratio and power consumption; secondly, the number of theoretical plates of the debutanizer is large, the pressure difference between the top of the tower and the tower at a low position is difficult to avoid obvious fluctuation in the operation process, the boiling point difference between the top and the low position is also obviously fluctuated, the operation stability of a heat pump system is influenced, and on the premise of effective operation and regulation of the tower, more complex control design is needed to avoid surge or choke of a heat pump compressor.
Patent CN107915580A proposes the use of multi-effect rectification in the de-butanol column. Because the ethylene glycol is easy to generate dehydration condensation reaction at higher temperature to generate diethylene glycol and triethylene glycol, the bottom temperature of the tower is usually controlled below 180 ℃, so the top pressure of the high-pressure debutanizer is usually not more than 0.5atm, the pressure of the low-pressure debutanizer is not too low, otherwise, the required tower diameter is too large, and the high-pressure and low-pressure step ranges are narrow. And the obvious pressure difference between the top of the tower and the bottom of the low-pressure debutanizer tower caused by large number of theoretical plates is also considered, so the available heat transfer temperature difference between the top of the high-pressure debutanizer tower and the bottom of the low-pressure debutanizer tower is very small, the method is only suitable for double-effect rectification, and the equipment investment with less than half of recovery energy consumption is huge.
The heat pump and the added compressor or tower equipment of the multi-effect rectification have certain operation control difficulty, meanwhile, the heat pump rectification couples the heat load adjusting operation condition of the top of the debutanizer tower and the bottom of the tower, and the multi-effect rectification couples the heat load adjusting operation condition of the top of the high-pressure debutanizer tower and the bottom of the low-pressure debutanizer tower, so that greater control system design and operation difficulty are brought, and the application of the energy-saving technologies in industrial practice is hindered.
Disclosure of Invention
The present invention is directed to overcoming the above-mentioned drawbacks of the prior art and providing an alternative thermal coupling process for vacuum induced air for ethylene glycol fractionation without the need for vapor delivery equipment and with easy control of operation.
The purpose of the invention can be realized by the following technical scheme: a replacement thermal coupling process of vacuum induced air for ethylene glycol rectification separation adopts a vacuum system to guide dihydric alcohol steam at the top of a debutanizer tower to exchange heat with a heated stream in a coupling way; the pressure of the dihydric alcohol steam is 0.2-0.6bar, and the dihydric alcohol steam is completely condensed by a coupling heat exchanger and a condenser which are connected in series, wherein the top part of the shell pass of the condenser, which is far away from the dihydric alcohol steam inlet, is connected with a vacuum system, the flow of the dihydric alcohol steam is guided by the vacuum system, and the pressure at the top of the de-butanol tower is adjusted; the heated stream is divided into two parts which are connected in parallel and are heated by a coupling heat exchanger and a heater respectively.
The coupling heat exchanger and the condenser adopt a shell-and-tube heat exchanger or a plate-and-shell heat exchanger, the glycol steam at the top of the de-butanol tower is introduced into the shell pass of the coupling heat exchanger, and the uncondensed part is led out from the top of the shell pass of the coupling heat exchanger and then introduced into the shell pass of the condenser;
the diameter of the glycol vapor along the path is selected so that the flow rate of glycol vapor from the top of the de-butanol column to the coupling heat exchanger is 10-30 m/s.
The structure form of the coupling heat exchanger is selected, so that the resistance pressure drop of glycol steam flowing through the shell side of the coupling heat exchanger is 3-15 kPa.
The glycol steam enters the coupling heat exchanger and enters the condenser, or condensate of the glycol steam is sprayed near the entrance of the condenser (the mass ratio of the condensate to the glycol steam is 1:1000-1:100) so as to ensure that the glycol steam entering the coupling heat exchanger and entering the condenser is in a saturated state rather than a superheated state.
The heated stream is a stream which needs to be heated in the ethylene glycol rectification process and comprises tower kettle liquid of a dehydration tower, a de-oxalate tower or an ethylene glycol refining tower or liquid extracted from the side line of a stripping section, or a liquid stream entering the dehydration tower, the de-oxalate tower or the ethylene glycol refining tower.
The condenser adopts circulating water CWI or other cooling media to ensure the cooling load of the driving of the top of the de-butanol tower and meet the cooling load change required by the adjustment of the operation process, the heater adopts STEAM STEAM or other heating media and is used for meeting the heating load of the driving of the working procedure where the heated stream is coupled and meeting the heating load change required by the adjustment of the operation process, the load of the coupling heat exchanger can simultaneously play a role in replacing and supplementing the cooling load of the condenser and the heating load of the heater in the operation process, and the load of the coupling heat exchanger is adjusted through a valve V1.
The coupling heat exchanger exchanges heat with one coupling heated stream by using glycol steam, or two groups of coupling heat exchangers connected in parallel are used as a supplementary reboiler of the ethylene glycol refining tower and exchange heat with the two coupling heated streams.
The cooling load of the condenser is designed according to 0.3-0.8 time of the cooling load of the glycol steam required by the production capacity; the heating load of the heater is designed according to the heating load of the coupled heated stream required by the production capacity, which is 0.3-0.8 times; the load of the coupling heat exchanger is designed according to the heating load of the heated stream required by the production capacity for coupling 0.5-1 times.
When the ethylene glycol rectification system runs at full load, the load of the coupling heat exchanger is controlled to be 0.6-0.9 time of the heating load of the coupled heated stream required by the production capacity, and the cooling load of the condenser is operated and regulated to be 0.1-0.8 time of the cooling load of the glycol steam required by the production capacity; the heating load of the heater is controlled by coupling 0.1-0.4 times of the heating load of the heated stream required by the production capacity.
And a valve is arranged on a connecting pipeline of the heated stream and the coupling heat exchanger.
Closing a valve when the ethylene glycol rectification system is started, condensing the glycol steam in a condenser after the glycol steam flows through a shell pass of a coupling heat exchanger, and heating the heated stream by a heater;
after the ethylene glycol rectification system is started at low load (0.3-0.8 times of the production capacity) and runs stably, gradually opening a valve, simultaneously replacing part of cooling load of a condenser and part of heating load of a heater with load of a coupling heat exchanger, and simultaneously respectively adjusting the cooling load at the top of the de-butanol tower and the heating load of a working procedure in which a coupled heated stream is located through the condenser and the heater according to needs;
then, the ethylene glycol rectification system is gradually increased from low-load operation (0.3-0.8 times of the production capacity) to full-load operation, the valve is continuously and gradually opened, the load of the coupling heat exchanger is used for simultaneously supplementing part of cooling load of the condenser and part of heating load of the heater, and simultaneously the cooling load at the top of the de-butanol tower and the heating load of a working procedure in which the heated stream is coupled are respectively adjusted through the condenser and the heater according to needs.
Compared with the prior art, the invention has the following beneficial effects:
1. because the temperature of the dihydric alcohol steam at the top of the de-butanol tower is about 150 ℃ under the normal operating pressure, the heat energy is wasted and extra cost is needed by directly adopting condensation water for condensation, the dihydric alcohol steam is necessary to be coupled with other working procedures needing to be heated in the ethylene glycol production process for realizing heat recovery, and the working procedures needing to be heated are mutually associated with the control operation at the top of the de-butanol tower due to the coupling influence of the coupling technology, so that the recovery and the utilization of the heat energy are very difficult, the invention carries out semi-decoupling design on the existing coupling relation, leads the dihydric alcohol steam S1 at the top of the de-butanol tower to pass through the coupling heat exchanger E-C and the condenser E1 which are connected in series, wherein the coupling heat exchanger E-C is coupled with other processes needing to be heated in the ethylene glycol refining process, and the heater E2 is additionally arranged at the process needing to be heated, the operation conditions of the tower top of the de-butanol and the working procedure of the coupled heated stream can be independently adjusted and controlled, the operational coupling is removed, the maximum recovery of the heat energy of the glycol steam is realized by controlling the loads of the coupling heat exchanger E-C, the condenser E1 and the heater E2, and the stable output of the set stable fluid in the semi-coupled heating working procedure is ensured.
2. The glycol vapor at the top of the debutanizer can be used for process-level external-domain thermal coupling, but glycol vapor is not amenable to direct compression and is limited by transport mechanical difficulties. Because the glycol steam can be condensed under very low pressure (the condensation pressure at 50 ℃ is less than 100Pa, the condensation pressure at 60 ℃ is less than 200Pa) and can be used as a valuable heating heat source in a certain pressure range (table 1), the glycol steam at the top of the de-butanol tower is guided to an adjacent tower by a vacuum system to be coupled with a heated stream for heat exchange. Meanwhile, the flow resistance of the dihydric alcohol steam is controlled by reasonably setting the pressure at the top of the de-butanol tower and setting a proper pipeline flow rate and a heat exchanger structural form, so that the higher saturation temperature of the dihydric alcohol steam in the coupling heat exchange process is ensured.
3. The invention avoids the use of a heat pump and a compressor or tower equipment added by multi-effect rectification, realizes independent adjustment and control of the operation conditions of the working procedures of the top of the butanol removal tower and the coupling heated stream by only adding a condenser and a heater, is simple and convenient, has low cost, and can effectively recover the heat energy of the dihydric alcohol steam at the top of the butanol removal tower.
Drawings
FIG. 1 is a schematic diagram of a replacement thermal coupling process for vacuum induced air for ethylene glycol rectification separation according to the present invention;
FIG. 2 is a schematic diagram of an alternative thermal coupling process for vacuum induced air for ethylene glycol fractionation in example 1;
FIG. 3 is a flow diagram of an alternative thermal coupling process for vacuum induced air for ethylene glycol fractionation in example 2.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments. The following examples are carried out on the premise of the technical scheme of the invention, and the embodiments and specific operation processes are given, but the scope of the invention is not limited to the following examples.
The invention relates to an ethylene glycol rectification system, which comprises a dehydration tower T1, an oxalate removal tower T2, a butanol removal tower T3 and an ethylene glycol refining tower T4, and is characterized in that a vacuum system is adopted to guide glycol steam at the top of the butanol removal tower to an adjacent tower to be coupled and heat-exchanged with a heated stream, and meanwhile, the pressure at the top of the butanol removal tower is reasonably set, and proper pipeline flow rate and heat exchanger structural form are set to control the flow resistance of the glycol steam, so that the glycol steam has higher saturation temperature in the coupling and heat exchange process, the heat energy of the gas discharged from the top of the butanol removal tower in the ethylene glycol rectification system is recycled, and meanwhile, the operation conditions of the process of the top of the butanol removal tower and the coupled heated stream can be independently adjusted and controlled, and the operational coupling is removed.
As shown in fig. 1, the glycol steam S1 at the top of the de-butanol tower passes through a coupling heat exchanger E-C and a condenser E1 connected in series to achieve complete condensation, the coupling heat exchanger E-C and the condenser E1 adopt shell-and-tube heat exchangers or plate-and-shell heat exchangers, the glycol steam S1 at the top of the de-butanol tower is introduced into the shell pass of the coupling heat exchanger E-C, the uncondensed portion S2 is led out from the top of the shell pass of E-C and then introduced into the shell pass of the condenser E1, the top of the shell pass of the condenser E1 far away from the glycol steam inlet is connected with a vacuum system P1, the glycol steam is guided by the vacuum system to flow through the coupling heat exchanger E-C and the condenser E1 from the top of the de-butanol tower to achieve condensation, and the pressure at the top of the de-butanol tower is adjusted; the fluid S3 condensed from the coupling heat exchanger E-C and the fluid S4 condensed from the condenser E1 are glycol condensate and are converged into a condensate storage tank B1, the coupled heated stream S5 is divided into two parts which are connected in parallel and heated by the coupling heat exchanger E-C and a heater E2, specifically, one path of the fluid S6 is heated fluid S9 after heat exchange through the coupling heat exchanger E-C, the other path of the fluid S7 is heated fluid S8 after being heated through a heater E2, and a branch where the fluid S6 is located is provided with a regulating valve V1; the heated stream S5 can be liquid at the bottom of a dehydration tower, a de-oxalate tower or an ethylene glycol refining tower or side-draw liquid at a stripping section, or can be a liquid feed stream entering the dehydration tower, the de-oxalate tower or the ethylene glycol refining tower;
the condenser E1 adopts circulating water CWI or other cooling media to ensure the cooling load of the start of the top of the butanol removal tower and meet the change of the cooling load required by the adjustment of the operation process, the heater E2 adopts STEAM STEAM or other heating media for meeting the requirements of the heating load of the start of the process in which the heated stream S5 is coupled and the change of the heating load required by the adjustment of the operation process, the load of the coupling heat exchanger E-C can play a role in replacing and supplementing the cooling load of the condenser E1 and the heating load of the heater E2 simultaneously in the operation process, and the load of the coupling heat exchanger E-C is adjusted through a valve V1;
the coupling heat exchanger E-C and the condenser E1 adopt a tube-shell heat exchanger or a plate-shell heat exchanger, the glycol steam S1 at the top of the de-butanol tower is introduced into the shell pass of the coupling heat exchanger E-C, the uncondensed part S2 is led out from the top of the shell pass of the E-C and then introduced into the shell pass of the condenser E1, the top of the shell pass of the E1 is connected with a vacuum system P1 to guide the glycol steam to flow through the coupling heat exchanger E-C and the condenser E1 from the top of the de-butanol tower to realize condensation, and the pressure at the top of the de-butanol tower is adjusted;
when the rectification system is started, the valve V1 is closed, the glycol steam S1 flows through the shell pass of the coupling heat exchanger E-C and then is condensed in the condenser E1, and the coupling heated stream S5 is heated by the heater E2; after the rectification system is started at low load (0.3-0.8 times of production capacity) and runs stably, a valve V1 is gradually opened, the load of a coupling heat exchanger E-C is used for simultaneously replacing part of cooling load of a condenser E1 and part of heating load of a heater E2, and simultaneously the cooling load at the top of the de-butanol tower and the heating load of a working procedure in which a coupled heated stream is located are respectively adjusted through a condenser E1 and a heater E2 according to needs; then, gradually increasing the rectifying system from low-load operation (0.3-0.8 times of the production capacity) to full-load operation, continuously and gradually opening a valve V1, simultaneously supplementing part of the cooling load of a condenser E1 and part of the heating load of a heater E2 by the load of a coupling heat exchanger E-C, and simultaneously respectively adjusting the cooling load at the top of the de-butanol tower and the heating load of a process in which a coupled heated stream is positioned through a condenser E1 and a heater E2 according to needs;
when the rectification system runs at full load, the load of the coupling heat exchanger E-C is controlled to be 0.6-0.9 time of the heating load of the coupling heated stream S5 required by the production capacity, and the cooling load of the condenser E1 is operated and regulated to be 0.1-0.8 time of the cooling load of the glycol steam S1 required by the production capacity; the heating load of heater E2 was operationally controlled at a capacity requirement coupled with the heating load of heated stream S5 from 0.1 to 0.4 times;
coupling heat exchanger E-C can be glycol vapor S1 in heat exchange with a coupled heated stream S5, such as a glycol finishing column reboiler; or two or more groups of heat exchangers connected in parallel can be adopted to realize the respective heat exchange of the glycol steam S1 and two or more coupled heated streams, such as the coupling with a reboiler of an ethylene glycol refining tower, and a feed preheater is arranged in a dehydration tower to realize the partial vaporization of the feed;
example 1
As shown in figure 2, stream S80 extracted from the bottom of the de-oxalate enters a de-butanol tower T3, the pressure of the de-butanol tower T3 is 0.4atm, the temperature is 162 ℃, glycol steam S1 at the top of the de-butanol tower T3 passes through a coupling heat exchanger E-C and a condenser E1 which are connected in series to realize total condensation, the condenser E1 adopts circulating water CWI to ensure the cooling load of the start-up of the de-butanol tower and meet the cooling load change required by the adjustment of the operation process, the condensate generated by the coupling heat exchanger E-C and the condenser E1 converges into a condensate storage tank B1, a mixed glycol product S14 is extracted, the rest part of S13 reflows to the top of the de-butanol tower T3, stream S11 extracted from the bottom of the de-butanol tower T3 enters an ethylene glycol refining tower T4, the pressure of the ethylene glycol refining tower T4 is 0.1atm, a product ethylene glycol S15 is extracted by a liquid side line S15, and a trace moisture generated by the top steam stream S17 is extracted, the bottom contains heavy components such as diethylene glycol, triethylene glycol and the like and ethylene glycol, and the temperature is 145 ℃;
the bottom liquid of the ethylene glycol refining tower T4 is used as a coupled heated stream (namely, a heated stream S5, not shown in the figure) and is divided into two parts which are connected in parallel, wherein one path of fluid S6 enters a coupling heat exchanger E-C, a regulating valve V1 is arranged on the branch, and the other path of fluid (namely, fluid S7, not shown in the figure) enters a reboiler of the ethylene glycol refining tower, namely, a heater E2 for heating; the heater E2 is heated by water vapor to meet the heating load of the start-up of the bottom of the ethylene glycol refining tower and the heating load change required by the adjustment in the operation process, the load of the coupling heat exchanger E-C can replace and supplement the cooling load of the condenser E1 and the heating load of the heater E2 in the operation process, and the load of the coupling heat exchanger E-C is adjusted by a valve V1;
the coupling heat exchanger E-C and the condenser E1 adopt tube-in-tube heat exchangers, glycol steam S1 is introduced into the shell pass of the coupling heat exchanger E-C, the uncondensed part S2 is led out from the top of the shell pass of the coupling heat exchanger E-C and then introduced into the shell pass of the condenser E1, the top of the shell pass of the condenser E1 is connected with a vacuum system P1 to guide the glycol steam to flow through the coupling heat exchanger E-C and the condenser E1 from the top of the de-butanol tower to realize condensation, and the pressure at the top of the de-butanol tower is adjusted;
the flow rate of the glycol vapor S1 from the top of the de-butanol to the coupling heat exchanger E-C was 15 m/S; the resistance pressure drop of the glycol vapor flowing through the shell side of the coupling heat exchanger E-C is 6 kPa; the condensed liquid of the glycol steam (the mass ratio of the condensed liquid to the glycol steam is 1:200) is sprayed near the inlet of the condenser E1 to eliminate the state of steam overheating caused by the flow resistance of the glycol steam flowing through the coupling heat exchanger E-C;
the cooling load of the condenser E1 was designed to be 0.9 times the cooling load of the glycol vapor S1 required for capacity; the heating load of the heater E2 is designed according to the reboiling heating load of the bottom of the ethylene glycol refining tower required by the production capacity, which is 0.7 times; the load of the coupling heat exchanger E-C is designed according to the reboiling heating load of the bottom of the ethylene glycol refining tower required by the production capacity, which is 0.8 times;
when the rectification system is started, the valve V1 is closed, the glycol steam S1 flows through the shell pass of the coupling heat exchanger E-C and then is condensed in the condenser E1, and the bottom of the glycol refining tower is reboiled and heated by a reboiler, namely a heater E2; after the rectification system is started at a low load of 0.5 time of the production capacity and runs stably, a valve V1 is gradually opened, the load of a coupling heat exchanger E-C is used for simultaneously replacing part of the cooling load of a condenser E1 and part of the reboiling heating load of a heater E2, and the cooling load at the top of the de-butanol tower and the reboiling heating load at the bottom of the ethylene glycol refining tower are respectively adjusted through a condenser E1 and a heater E2 according to needs; then, the rectifying system is gradually increased from 0.5 times of low-load operation to full-load operation, during which, a valve V1 is continuously and gradually opened, the load of the coupling heat exchanger E-C is used for simultaneously supplementing part of the cooling load of a condenser E1 and part of the heating load of a reboiler E2, and simultaneously, the cooling load at the top of the de-butanol tower and the reboiling heating load at the bottom of the glycol refining tower are respectively adjusted through a condenser E1 and a reboiler E2 according to requirements;
when the rectifying system runs at full load, the cooling load of the glycol steam S1 is 1.5 times of the reboiling heating load at the bottom of the glycol refining tower, the load of the coupling heat exchanger E-C is controlled to be 0.6 times of the reboiling heating load at the bottom of the glycol refining tower, and the cooling load of the condenser E1 is operated and regulated at 0.65 times of the cooling load of the glycol steam S1 required by the production capacity; the heating load of the reboiler E2 was operated and controlled at 0.4 times the reboiling heating load required for the production capacity; the latent heat of condensation recovery ratio of the glycol vapor was 53%.
Example 2
As shown in figure 3, a condensed liquid product FEED from an oxalate hydrogenation reaction section has the temperature of 90 ℃, enters a dehydration tower T1 after passing through a coupling heat exchanger E-CA, the top pressure of the dehydration tower T1 is 0.6atm, a stream S20 of light components such as water and methanol and the like is produced at the top of the dehydration tower T1, a stream S19 at the bottom of the dehydration tower T1 enters a de-oxalate tower T2, the top pressure of the de-oxalate tower T2 is 0.5atm, a stream S18 mainly comprising oxalate and methyl glycolate is produced at the top of the de-oxalate tower T2, a stream S80 produced at the bottom of the tower enters a de-butanol tower T3, the top pressure of the de-butanol tower T3 is 0.4atm, the temperature is 162 ℃, binary alcohol steam at the top of the de-butanol tower T3 is divided into two parts of S1 and S1A which are connected in parallel, the coupling heat exchanger E-C and the coupling heat exchanger E-CA are respectively introduced into the coupling heat exchanger E-C and the coupling heat exchanger E1, and the condensation steam S22 of the coupling heat exchanger E-CA are connected in parallel to realize the condensation condenser in parallel, the condenser E1 adopts circulating water CWI to ensure the cooling load of the start of the top of the de-butanol tower and meet the cooling load change required by the adjustment of the operation process, the condensate S3 of the coupling heat exchanger E-C, the condensate S3A of the coupling heat exchanger E-CA and the condensate S4 of the condenser E1 are converged into a condensate storage tank B1, a mixed dihydric alcohol product S14 is extracted, the rest part of S13 reflows to the top of the de-butanol tower T3, a stream S11 extracted from the bottom of the de-butanol tower T3 enters an ethylene glycol refining tower T4, the top pressure of the ethylene glycol refining tower T4 is 0.1atm, a product ethylene glycol is extracted from a side line S15, a trace amount of moisture generated by the condensation of ethylene glycol extracted from a top steam stream S17 is reflowed to a dehydrating tower T1, and a stream S12 at the bottom contains heavy components such as diethylene glycol and triethylene glycol and ethylene glycol, and the temperature is 175 ℃; wherein, the glycol steam S1A at the top of the de-butanol tower T3 enters a branch of a condenser E1 after entering a coupling heat exchanger E-CA and is provided with a regulating valve V2.
The flow rate of the glycol vapor S1 from the top of the debutanizer to the coupling heat exchanger E-C was 18m/S, and the flow rate of the glycol vapor S1A from the top of the debutanizer to the coupling heat exchanger E-CA was 18 m/S; the resistance pressure drop of glycol steam flowing through the E-C shell pass of the coupling heat exchanger is 12kPa, the resistance pressure drop of glycol steam flowing through the E-CA shell pass of the coupling heat exchanger is 6kPa, and the resistance pressure drop of glycol steam flowing through the regulating valve V2 is 6 kPa; the condensed liquid of the glycol steam (the mass ratio of the condensed liquid to the glycol steam is 1:200) is sprayed near the inlet of the condenser E1 to eliminate the state of steam overheating caused by the flow resistance of the glycol steam flowing through the coupling heat exchanger E-C or E-CA; spraying condensate of the glycol steam (the mass ratio of the condensate to the glycol steam is 1:1000) near the inlet of the coupling heat exchanger E-CA to eliminate the state of steam overheating caused by the on-way flow resistance of the glycol steam S1A;
the liquid S6 extracted from the side of the stripping section of the ethylene glycol refining tower T4 is used as one of coupled heated streams, the temperature is 142 ℃, supplementary reboiling heat load is provided by coupling heat exchangers E-C, and the heating load of the kettle of the ethylene glycol refining tower is provided by the ethylene glycol refining tower reboiler E2; the reboiler E2 adopts 1.6MPa steam for heating to meet the heating load of the start-up of the bottom of the ethylene glycol coupling refining tower and the heating load change required by the adjustment in the operation process, the load of the coupling heat exchanger E-C can replace and supplement the cooling load of the condenser E1 and the heating load of the reboiler E2 in the operation process, and the load of the coupling heat exchanger E-C is adjusted through a valve V1;
dehydration column T1 FEED fed and as a second part of the coupled heated stream, dehydration column T1 FEED fed was preheated by coupling heat exchanger E-CA whose duty can supplement or replace the reboiling heating duty of reboiler E2A at the bottom of dehydration column T1; the reboiler E2A adopts 1.6MPa steam to heat the heating load for the full dehydration tower bottom start-up and meet the heating load change required by the adjustment in the operation process, the load of the coupling heat exchanger E-CA can replace and supplement the cooling load of the condenser E1 and the heating load of the reboiler E2A in the operation process, and the load of the coupling heat exchanger E-CA is adjusted through a valve V2;
the coupling heat exchanger E-C, the coupling heat exchanger E-CA and the condenser E1 adopt tube-in-tube heat exchangers, glycol steam S1 is introduced into the shell pass of the coupling heat exchanger E-C, uncondensed part S2 is led out from the top of the shell pass of the coupling heat exchanger E-C and then introduced into the shell pass of the condenser E1, glycol steam S1A is introduced into the shell pass of the coupling heat exchanger E-CA, uncondensed part S22 is led out from the top of the shell pass of the coupling heat exchanger E-C and then introduced into the shell pass of the condenser E1, the top of the shell pass of the condenser E1 is connected with a vacuum system P1 to guide glycol steam to flow through the coupling heat exchanger E-C or the coupling heat exchanger ECA from the top of the de-butanol tower and then enter the condenser E1 to realize condensation and adjust the pressure at the top of the de-butanol tower;
the cooling load of the condenser E1 was designed to be 0.7 times the cooling load required for the production capacity for the entire condensation of the glycol vapors S1 and S1A; the heating load of the heater E2 is designed according to the reboiling heating load of the bottom of the ethylene glycol refining tower required by the production capacity, which is 0.7 times; the heating load of the heater E2A was designed according to the reboiling heating load at the bottom of the dehydration column required for the production capacity, which was 0.8 times; the load of the coupling heat exchanger E-C is designed according to the reboiling heating load at the bottom of the ethylene glycol refining tower required by the production capacity; the load of the coupling heat exchanger E-CA is designed according to the reboiling heating load at the bottom of the dehydration tower required by the production capacity, the FEED stream can be heated to 115 ℃ at 0.6atm, and the vaporization mass fraction is 0.12;
when the rectification system is started, the regulating valve V1 and the regulating valve V2 are closed, the glycol steam flows through the shell pass of the coupling heat exchanger E-C and then is condensed in the condenser E1, and the bottom of the glycol refining tower is reboiled and heated by the heater E2 (namely a reboiler); after the rectification system is started at a low load of 0.5 time of the production capacity and runs stably, a regulating valve V1 is gradually opened, the load of a coupling heat exchanger E-C is used for simultaneously replacing part of cooling load of a condenser E1 and part of reboiling heating load of a heater E2, and simultaneously the cooling load at the top of a de-butanol tower and the reboiling heating load at the bottom of an ethylene glycol refining tower are respectively regulated through a condenser E1 and a heater E2 according to needs; then, gradually opening an adjusting valve V2, continuously replacing part of cooling load of a condenser E1 with load of a coupling heat exchanger E-CA, reducing part of reboiling heating load of a reboiler E2A, and respectively adjusting cooling load at the top of the de-butanol tower and reboiling heating load at the bottom of the dehydration tower through a condenser E1 and a heater E2A according to needs; then, the rectification system is gradually increased from 0.5 times of low-load operation to full-load operation, and the regulating valve V1 and the regulating valve V2 are continuously and gradually opened during the period, the load of the coupling heat exchanger E-C is used for simultaneously supplementing a part of cooling load of the condenser E1 and a part of heating load of the heater E2, the load of the coupling heat exchanger E-CA is used for simultaneously supplementing a part of cooling load of the condenser E1 and reducing a part of heating load of the heater E2A, and simultaneously the cooling load at the top of the butanol removal tower and the reboiling heating load at the bottom of the dehydration tower are respectively regulated through the condenser E1 and the heater E2A according to needs;
when the rectifying system runs at full load, the cooling and condensing load required by the glycol steam S1 is 1 time of the reboiling heating load at the bottom of the glycol refining tower, the cooling and condensing load required by the glycol steam S1A is 1 time of the vaporizing heating load at the feeding part of the dehydrating tower, the load of the coupling heat exchanger E-C is controlled at 0.8 time of the reboiling heating load at the bottom of the glycol refining tower, the load of the coupling heat exchanger E-CA is controlled at 0.4 time of the reboiling heating load at the bottom of the dehydrating tower, and the cooling load of the condenser E1 is operated and regulated at 0.2 time of the cooling load of the glycol steam S1 required by the production capacity; the heating load of the heater E2 is operated and regulated at 0.2 time of the reboiling heating load required by the production capacity, and the heating load of the heater E2A is operated and regulated at 0.6 time of the reboiling heating load required by the production capacity; the latent heat of condensation recovery ratio of the glycol vapor was 80%.
Claims (7)
1. A replacement thermal coupling process of vacuum induced air for ethylene glycol rectification separation is characterized in that a vacuum system is adopted to guide glycol steam (S1) at the top of a debutanizer to be coupled with a heated stream (S5) for heat exchange; the pressure of the glycol steam (S1) is 0.2-0.6bar, and the glycol steam is completely condensed by sequentially passing through a coupling heat exchanger (E-C) and a condenser (E1) which are connected in series, wherein the top part of the shell side of the condenser (E1) far away from a glycol steam inlet is connected with a vacuum system (P1), the flow of the glycol steam is guided by the vacuum system (P1), and the pressure of the top of a de-butanol tower is adjusted; the heated stream (S5) is divided into two parts in parallel, and the two parts are respectively heated by a coupling heat exchanger (E-C) and a heater (E2);
the heated stream (S5) comes from streams needing to be heated in the ethylene glycol rectification process, and comprises tower bottom liquid of a dehydration tower, a de-oxalate tower or an ethylene glycol refining tower or side-draw liquid of a stripping section, or liquid streams entering the dehydration tower, the de-oxalate tower or the ethylene glycol refining tower;
a valve (V1) is arranged on a connecting pipeline of the heated stream (S5) and the coupling heat exchanger (E-C);
when the ethylene glycol rectification system is started, a valve (V1) is closed, glycol steam (S1) flows through a shell pass of a coupling heat exchanger (E-C) and then is condensed in a condenser (E1), and a heated stream (S5) is heated by a heater (E2);
after the ethylene glycol rectification system is started at low load and operates stably, a valve (V1) is gradually opened, the load of a coupling heat exchanger (E-C) is used for simultaneously replacing part of the cooling load of a condenser (E1) and part of the heating load of a heater (E2), and the cooling load at the top of the de-butanol tower and the heating load of a process in which a heated stream (S5) is coupled are respectively adjusted through the condenser (E1) and the heater (E2) according to needs;
thereafter, the ethylene glycol rectification system is gradually increased from low load operation to full load operation, and the valve (V1) is continuously and gradually opened, the load of the coupling heat exchanger (E-C) is used for simultaneously supplementing part of the cooling load of the condenser (E1) and part of the heating load of the heater (E2), and simultaneously the cooling load of the top of the de-butanol tower and the heating load of the process in which the heated stream (S5) is coupled are respectively adjusted through the condenser (E1) and the heater (E2) according to needs.
2. The alternative thermal coupling process for vacuum induced air for ethylene glycol rectification separation according to claim 1 wherein the coupled heat exchangers (E-C) exchange heat with the glycol vapor a coupled heated stream or employ two sets of coupled heat exchangers in parallel as a supplemental reboiler for the ethylene glycol refining column while exchanging heat with both coupled heated streams.
3. The process of claim 1, wherein the flow rate of the glycol vapor (S1) from the top of the de-butanol column to the coupling heat exchanger (E-C) is 10-30 m/S.
4. The process of claim 1, wherein the glycol vapor (S1) flows through the shell side of the coupling heat exchanger (E-C) with a drag pressure drop of 3-15 kPa.
5. The alternative thermal coupling process for vacuum induced air for ethylene glycol rectification separation according to claim 1, characterized in that the glycol vapor (S1) enters the coupling heat exchanger (E-C) and enters the condenser (E1) and the condensate of the glycol vapor is sprayed at the inlet of the coupling heat exchanger (E-C) and the condenser (E1) so that the glycol vapor entering the coupling heat exchanger (E-C) and the condenser (E1) is in a saturated state.
6. The alternative thermal coupling process for vacuum induced draft for ethylene glycol fractionation according to claim 1 wherein the cooling duty of the condenser (E1) is designed to be 0.3 to 0.8 times the cooling duty of the glycol vapor (S1) required for production capacity; the heating load of the heater (E2) is designed according to the heating load of the coupled heated stream (S5) required by the production capacity, which is 0.3-0.8 times; the load of the coupling heat exchanger (E-C) is designed according to the heating load of the coupled heated stream (S5) required by the production capacity, which is 0.5-1 times.
7. The replacement thermal coupling process of vacuum induced air for ethylene glycol rectification separation according to claim 1, characterized in that when the ethylene glycol rectification system is in full-load operation, the load of the coupling heat exchanger (E-C) is controlled to be 0.6-0.9 times the heating load of the heated stream (S5) for coupling required for production capacity, and the cooling load of the condenser (E1) is regulated and controlled to be 0.1-0.8 times the cooling load of the glycol steam (S1) for production capacity; the heating duty of the heater (E2) was operatively regulated at the coupling required for the production capacity between 0.1 and 0.4 times the heating duty of the heated stream (S5).
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| CN104788289B (en) * | 2015-03-24 | 2017-06-13 | 惠生工程（中国）有限公司 | A kind of pump coupled heat technique of ethylene glycol rectifying |
| CN105330514B (en) * | 2015-10-12 | 2017-06-16 | 天津衡创工大现代塔器技术有限公司 | A kind of purifying technique of synthesis gas preparing ethylene glycol |
| CN105622337B (en) * | 2016-02-04 | 2020-11-17 | 天津大学 | Novel reactive distillation coupling process and device for separating liquid-phase product of ethylene glycol prepared from coal |
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| CN111592446A (en) * | 2020-06-10 | 2020-08-28 | 东华工程科技股份有限公司 | Rectification system and process for preparing ethylene glycol by dimethyl oxalate hydrogenation |
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