CN220386515U - Energy-saving system for treating isobutane dehydrogenation raw material - Google Patents
Energy-saving system for treating isobutane dehydrogenation raw material Download PDFInfo
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- CN220386515U CN220386515U CN202321857718.3U CN202321857718U CN220386515U CN 220386515 U CN220386515 U CN 220386515U CN 202321857718 U CN202321857718 U CN 202321857718U CN 220386515 U CN220386515 U CN 220386515U
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- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 title claims abstract description 102
- 238000006356 dehydrogenation reaction Methods 0.000 title claims abstract description 67
- 239000002994 raw material Substances 0.000 title claims abstract description 55
- 239000001282 iso-butane Substances 0.000 title claims abstract description 51
- 238000006317 isomerization reaction Methods 0.000 claims abstract description 62
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims abstract description 57
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical group COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000001273 butane Substances 0.000 claims abstract description 49
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000001257 hydrogen Substances 0.000 claims abstract description 48
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 48
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 46
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 38
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000000605 extraction Methods 0.000 claims abstract description 27
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 20
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims description 19
- 239000012492 regenerant Substances 0.000 claims description 6
- 125000004435 hydrogen atom Chemical group [H]* 0.000 claims description 3
- 238000004064 recycling Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 10
- 238000005516 engineering process Methods 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract 1
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 16
- 238000000034 method Methods 0.000 description 9
- 239000006227 byproduct Substances 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 125000004122 cyclic group Chemical group 0.000 description 4
- 239000003502 gasoline Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 150000001721 carbon Chemical class 0.000 description 2
- -1 carbon four Chemical compound 0.000 description 2
- 238000006392 deoxygenation reaction Methods 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000003254 gasoline additive Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
Classifications
-
- 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
- Y02P20/10—Process efficiency
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model provides an energy-saving system for treating isobutane dehydrogenation raw materials, which comprises a carbon four raw material pretreatment unit, a butane isomerization unit, a PSA hydrogen extraction unit, a dehydrogenation unit, a deoxidization and hydrogenation unit and an MTBE unit; the pretreatment unit of the carbon four raw materials is connected with the butane isomerization unit through a pipeline, the PSA hydrogen extraction unit is connected with the pretreatment unit of the carbon four raw materials, the butane isomerization unit is connected with the dehydrogenation unit through a pipeline, the dehydrogenation unit is connected with the PSA hydrogen extraction unit, the deoxidization and hydrogenation unit is connected with the butane isomerization unit through a pipeline, the dehydrogenation unit is connected with the MTBE unit, and the MTBE unit is connected with the deoxidization and hydrogenation unit through a pipeline. The utility model has the beneficial effects that: compared with the prior art, the technology reduces one tower, optimizes the operation parameters of the heterogeneous DIB tower, saves the energy consumption cost by about 4-20%, improves the energy utilization and greatly reduces the energy consumption.
Description
Technical Field
The utility model belongs to the technical field of chemical synthesis, and particularly relates to an energy-saving system for treating isobutane dehydrogenation raw materials.
Background
The MTBE used as the gasoline additive has excellent performance, not only has higher net octane number, but also has good blending effect on straight-run gasoline, alkylated gasoline, catalytic cracking gasoline, catalytic reforming gasoline and the like, and has higher blending octane number, thus having wide market prospect.
Isobutene has been the main raw material for MTBE synthesis, and in recent years, production cost pressure has been increasing, and even though production yield has been improved, isobutene is still in a state of being in short supply, and a part of demand depends on import. In recent years, the supply end of mixed butane is increased, and the price is lower. Therefore, isobutene can be prepared by dehydrogenation of isobutane, n-butane is converted into isobutane through isomerization, and the isobutene is used as a raw material to synthesize the MTBE with high added value.
The mature process which is operated at present takes mixed butane as a raw material, removes impurities such as olefin and the like through a carbon four raw material pretreatment unit, refines carbon four, enters a butane isomerization unit to carry out isomerization reaction, returns the isomerized carbon four to an isomerization unit to be separated by an isobutane removal tower (DIB tower), and enters an isobutane dehydrogenation unit, and returns normal butane to the butane isomerization unit to continue isomerization reaction; and the dehydrogenated carbon four is used as a raw material for synthesizing MTBE, enters an MTBE unit to produce an MTBE product, and the produced byproduct ether returns to an isobutane dehydrogenation unit after being deoxidized by an ORU unit and dehydrogenated by a CSP unit.
The traditional raw material pretreatment, butane isomerization, dehydrogenation process, ORU and CSP adopted in the prior art are used for producing raw material isobutene for MTBE synthesis, and the problems of complex process flow, large investment and high energy consumption exist.
Disclosure of Invention
In view of the above, the utility model aims to provide an energy-saving system for treating an isobutane dehydrogenation raw material, so as to solve the problems of complex process flow, large investment and high energy consumption in the traditional raw material pretreatment, butane isomerization, dehydrogenation process, ORU and CSP production of raw material isobutene for MTBE synthesis.
In order to achieve the above purpose, the technical scheme of the utility model is realized as follows:
an energy-saving system for treating isobutane dehydrogenation raw materials comprises a carbon four raw material pretreatment unit, a butane isomerization unit, a PSA hydrogen extraction unit, a dehydrogenation unit, a deoxidization and hydrogenation unit and an MTBE unit;
the pretreatment unit of the carbon four raw materials is connected with the butane isomerization unit through a pipeline, the PSA hydrogen extraction unit is connected with the pretreatment unit of the carbon four raw materials, the butane isomerization unit is connected with the dehydrogenation unit through a pipeline, the dehydrogenation unit is connected with the PSA hydrogen extraction unit, the deoxidization and hydrogenation unit is connected with the butane isomerization unit through a pipeline, the dehydrogenation unit is connected with the MTBE unit, and the MTBE unit is connected with the deoxidization and hydrogenation unit through a pipeline.
Further, a raw material feeding carbon four pipeline is arranged on the carbon four raw material pretreatment unit, and the carbon four raw material pretreatment unit is connected with the butane isomerization unit through a refined carbon four pipeline.
Further, the butane isomerization unit comprises an isomerization DIB tower and a butane isomerization device, wherein a refined carbon four pipeline is connected with the isomerization DIB tower, the top of the isomerization DIB tower is connected with the dehydrogenation unit through a refined isobutane outlet pipeline, the isomerization DIB tower is connected with the butane isomerization device through a normal butane outlet pipeline, and the isomerization DIB tower is connected with the butane isomerization device through a mixed butane inlet pipeline.
Furthermore, the top of the isomerism DIB tower is not provided with a tower top condenser, the isomerism DIB tower adopts heat pump rectification, and the tower top gas isobutane is used as a tower kettle reboiler heat source after being pressurized and heated by a compressor, so that compared with the traditional DIB tower, the tower top condenser is omitted, most of tower kettle steam consumption is saved, the investment is reduced, and the energy consumption is reduced.
Further, the PSA hydrogen extraction unit is connected with the butane isomerization device through a first hydrogen inlet pipeline, and the PSA hydrogen extraction unit is connected with the four-carbon raw material pretreatment unit through a second hydrogen inlet pipeline. The PSA hydrogen extraction unit supplies hydrogen for the carbon four raw material pretreatment unit and the butane isomerization unit, and refines crude hydrogen generated by the dehydrogenation unit.
Further, the dehydrogenation unit is connected with the PSA hydrogen extraction unit through a crude hydrogen outlet line. And (3) refining isobutane in the dehydrogenation unit for dehydrogenation, wherein the generated crude hydrogen enters the PSA hydrogen extraction unit, and the dehydrogenated carbon four enters the MTBE unit.
Further, the deoxygenation and hydrogenation unit comprises a CSP unit and a 0RU unit, the 0RU unit is connected to the CSP unit by a first recycle isobutane line, and the CSP unit is connected to the heterogeneous DIB column by a second recycle isobutane line.
Further, the 0RU unit is connected to the MTBE unit by a recycle regenerant outlet line and the MTBE unit is connected to the 0RU unit by an ether outlet isobutane line.
Further, the MTBE unit is provided with a methyl tertiary butyl ether outlet pipeline. The dehydrogenation carbon four in the MTBE unit reacts with methanol to generate MTBE, and the byproduct ether, namely carbon four, enters a CSP device and a 0RU device. And the CSP device and the 0RU device remove trace oxides and hydrogenate the carbon four after the ether, and the generated circulating isobutane enters an isomerism DIB tower for separation. The CSP device is a saturated hydrogenation device, and the 0RU device is a trace oxide removal device.
For the prior art, the energy-saving system for treating the isobutane dehydrogenation raw material has the following advantages:
the utility model provides a method for recycling raw materials, namely a raw material C-IV raw material pretreatment unit, a butane isomerization unit and a dehydrogenation unit, which enter an MTBE unit to generate a product MTBE, and a byproduct, namely ether, is subjected to hydrotreating by a CSP device and a 0RU device. Compared with the prior art, the technology reduces one tower, optimizes the operation parameters of the heterogeneous DIB tower, saves the energy consumption cost by about 4-20%, improves the energy utilization and greatly reduces the energy consumption.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model. In the drawings:
FIG. 1 is a schematic diagram of an energy saving system for treating isobutane dehydrogenation feed according to an embodiment of the present utility model.
Reference numerals illustrate:
1. a carbon four raw material pretreatment unit; 2. an isomerised DIB column; 3. butane isomerization unit; 4. a PSA hydrogen extraction unit; 5. a dehydrogenation unit; 6. an MTBE unit; 7. a CSP device; 8. 0RU device.
Detailed Description
It should be noted that, without conflict, the embodiments of the present utility model and features of the embodiments may be combined with each other.
In the description of the present utility model, it should be understood that the terms "center", "longitudinal", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc. indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, are merely for convenience in describing the present utility model and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present utility model. Furthermore, the terms "first," "second," and the like, are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defining "a first", "a second", etc. may explicitly or implicitly include one or more such feature. In the description of the present utility model, unless otherwise indicated, the meaning of "a plurality" is two or more.
In the description of the present utility model, it should be noted that, unless explicitly specified and limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; can be directly connected or indirectly connected through an intermediate medium, and can be communication between two elements. The specific meaning of the above terms in the present utility model can be understood by those of ordinary skill in the art in a specific case.
The utility model will be described in detail below with reference to the drawings in connection with embodiments.
As shown in fig. 1, an energy saving system for treating isobutane dehydrogenation raw materials comprises a carbon four raw material pretreatment unit 1, a butane isomerization unit, a PSA hydrogen extraction unit 4, a dehydrogenation unit 5, an oxygen removal and hydrogenation unit and an MTBE unit 6; the pretreatment unit 1 for the carbon four raw materials is connected with the butane isomerization unit through a pipeline, the PSA hydrogen extraction unit 4 is connected with the pretreatment unit 1 for the carbon four raw materials, the butane isomerization unit is connected with the dehydrogenation unit 5 through a pipeline, the dehydrogenation unit 5 is connected with the PSA hydrogen extraction unit 4, the deoxidization and hydrogenation unit is connected with the butane isomerization unit through a pipeline, the dehydrogenation unit 5 is connected with the MTBE unit 6, and the MTBE unit 6 is connected with the deoxidization and hydrogenation unit through a pipeline.
The carbon four raw material pretreatment unit 1 is provided with a raw material feeding carbon four pipeline, and the carbon four raw material pretreatment unit 1 is connected with a butane isomerization unit through a refined carbon four pipeline.
The butane isomerization unit comprises an isomerization DIB tower 2 and a butane isomerization device 3, wherein a refined carbon four pipeline is connected with the isomerization DIB tower 2, the top of the isomerization DIB tower 2 is connected with a dehydrogenation unit 5 through a refined isobutane outlet pipeline, the isomerization DIB tower 2 is connected with the butane isomerization device 3 through a normal butane outlet pipeline, and the isomerization DIB tower 2 is connected with the butane isomerization device 3 through a mixed butane inlet pipeline.
The top of the isomerism DIB tower 2 is not provided with a tower top condenser, the isomerism DIB tower 2 adopts a heat pump for rectification, and the pressure and the temperature of the tower top gas-phase isobutane are raised by a compressor and then are used as a tower kettle reboiler heat source, so that compared with the traditional DIB tower, the tower top condenser is omitted, most of tower kettle steam consumption is saved, the investment is reduced, and the energy consumption is reduced.
The PSA hydrogen extraction unit 4 is connected with the butane isomerization device 3 through a first hydrogen inlet pipeline, and the PSA hydrogen extraction unit 4 is connected with the four-carbon raw material pretreatment unit 1 through a second hydrogen inlet pipeline.
The dehydrogenation unit 5 is connected to the PSA hydrogen unit 4 by a crude hydrogen outlet line.
The deoxygenation and hydrogenation unit comprises CSP unit 7 and 0RU unit 8,0RU unit 8 connected to CSP unit 7 by a first recycle isobutane line and CSP unit 7 connected to heterogeneous DIB column 2 by a second recycle isobutane line. The CSP device is a saturated hydrogenation device, and the 0RU device is a trace oxide removal device.
The 0RU unit 8 is connected to the MTBE unit 6 by a recycle regenerant outlet line, and the MTBE unit 6 is connected to the 0RU unit 8 by an after-ether isobutane outlet line.
The MTBE unit 6 is provided with a methyl tert-butyl ether line.
Example 1:
the method comprises the steps that raw material C four firstly reacts with hydrogen from a PSA hydrogen extraction unit to enter a C four raw material pretreatment unit, the generated refined C four and circulating isobutane from a CSP device and a 0RU device are separated by entering an isomerism DIB tower from different tower plate positions, normal butane collected from a side line is subjected to isomerism reaction with the hydrogen, the generated mixed butane returns to the isomerism DIB tower again to be separated, refined isobutane generated from the tower top enters a dehydrogenation unit to be dehydrogenated, crude hydrogen generated from the dehydrogenation reaction enters a PSA hydrogen extraction unit to be refined, the generated dehydrogenated C four is used as raw material of an MTBE unit to generate an MTBE product, the C four after byproduct ether of the MTBE unit enters a CSP device and a 0RU device, trace oxide is removed, circulating isobutane generated by hydrogenation enters the DIB tower to be separated, and circulating regenerant generated by the 0RU device enters the MTBE unit to be separated.
Taking the route of this system as an example, a 40 ten thousand ton dehydrogenation (in terms of isobutylene produced by dehydrogenation) unit, its utility consumption is shown in Table 1 below:
the price steam of public engineering is 300 yuan/t, electricity is 0.8 yuan/kW.h, circulating water is 0.2 yuan/t, boiler feed water is 12 yuan/t, and fuel gas is 4 yuan/Nm 3 The cost of the utility is 87361 yuan/h.
Comparative example 1
The method comprises the steps that raw material C-IV firstly reacts with hydrogen from a PSA hydrogen extraction unit to enter a C-IV raw material pretreatment unit, the generated refined C-IV enters an isomerism DIB tower to be separated, normal butane collected from a side line is subjected to isomerisation reaction with the hydrogen, the generated mixed butane returns to the isomerism DIB tower again to be separated, refined isobutane generated from the top of the tower enters a dehydrogenation unit to be dehydrogenated, crude hydrogen generated from the dehydrogenation reaction enters the PSA hydrogen extraction unit to be refined, the generated dehydrogenated C-IV is used as raw material of an MTBE unit to generate MTBE product, the byproduct ether of the MTBE unit enters ORU and CSP unit, trace oxide and cyclic isobutane generated from hydrogenation are removed to enter the dehydrogenation DIB tower to be separated, cyclic regenerant generated from the ORU unit enters the MTBE unit to be separated, and cyclic isobutane generated from the CSP unit enters the dehydrogenation DIB tower to be separated, and the separated cyclic isobutane is subjected to dehydrogenation reaction.
According to this route, for example, a 40 ten thousand ton dehydrogenation (in terms of isobutene produced by dehydrogenation) unit, its utility consumption is given in Table 2 below:
the price steam of public engineering is 300 yuan/t, electricity is 0.8 yuan/kW.h, circulating water is 0.2 yuan/t, boiler feed water is 12 yuan/t, and fuel gas is 4 yuan/Nm 3 The cost of the utility is 90977 yuan/h.
As is clear from comparative example 1 and comparative example, the dehydrogenation DIB column was omitted, the diameter of the heterogeneous DIB column was enlarged and the pressure was reduced, the energy consumption cost was reduced by 3616 yuan/h, the annual operation time was 8000 hours, and the annual energy saving cost was 2892.8 ten thousand yuan/year.
Example 2
The method comprises the steps that raw material C four firstly reacts with hydrogen from a PSA hydrogen extraction unit to enter a C four raw material pretreatment unit, the generated refined C four and circulating isobutane from a CSP device and a 0RU device enter an isomerism DIB tower from different tower plate positions to be separated, the isomerism DIB tower adopts a heat pump rectification technology, tower top gas isobutane is pressurized and heated by a compressor and then serves as a tower kettle reboiler heat source, n-butane and hydrogen in the tower kettle are subjected to isomerisation reaction, the generated mixed butane returns to the DIB tower again to be separated, refined isobutane generated at the tower top enters a dehydrogenation unit to be dehydrogenated, crude hydrogen generated by the dehydrogenation reaction enters the PSA hydrogen extraction unit to be refined, the generated dehydrogenated C four is used as raw material of the MTBE unit to generate MTBE products, C four enters the CSP device and the 0RU device after being subjected to byproduct ether of the MTBE unit, trace oxide removal and circulating isobutane generated by hydrogenation enter the DIB tower to be separated, and circulating regenerant generated by the 0RU device enters the MTBE unit to be separated.
Taking the route of this system as an example, a 40 ten thousand ton dehydrogenation (in terms of isobutylene produced by dehydrogenation) unit, its utility consumption is shown in Table 3 below:
the price steam of public engineering is 300 yuan/t, electricity is 0.8 yuan/kW.h, circulating water is 0.2 yuan/t, boiler feed water is 12 yuan/t, and fuel gas is 4 yuan/Nm 3 Calculated, utility cost is 73645 yuan/h.
Example 2 is based on example 1 by using heat pump distillation technology on the isomerised DIB column, with a steam saving of 62t/h. The heat pump rectification is adopted, and the heat of the isobutane refined in the tower top gas phase is used as a heat source of a tower bottom reboiler, so that the heat is fully utilized, low-pressure steam needed by the tower bottom is reduced, and the steam consumption is greatly reduced.
In comparative example 2 and comparative example, the production energy consumption cost was reduced by 17332 yuan/h, and the annual operation time was measured at 8000 hours, and the annual energy saving cost was 13865.6 ten thousand yuan/year.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the utility model.
Claims (9)
1. An energy saving system for treating isobutane dehydrogenation feed stock, characterized by: comprises a carbon four raw material pretreatment unit (1), a butane isomerization unit, a PSA hydrogen extraction unit (4), a dehydrogenation unit (5), an deoxidization and hydrogenation unit and an MTBE unit (6);
the four raw materials pretreatment unit of carbon (1) is connected with butane isomerization unit through the pipeline, PSA draws hydrogen unit (4) to be connected with four raw materials pretreatment unit of carbon (1), butane isomerization unit is connected with dehydrogenation unit (5) through the pipeline, dehydrogenation unit (5) are connected with PSA draws hydrogen unit (4), deoxidization and hydrogenation unit are connected with butane isomerization unit through the pipeline, dehydrogenation unit (5) are connected with MTBE unit (6), MTBE unit (6) are connected with deoxidization and hydrogenation unit through the pipeline.
2. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the carbon four raw material pretreatment unit (1) is provided with a raw material feeding carbon four pipeline, and the carbon four raw material pretreatment unit (1) is connected with the butane isomerization unit through a refined carbon four pipeline.
3. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the butane isomerization unit comprises an isomerization DIB tower (2) and a butane isomerization device (3), wherein a refined carbon four pipeline is connected with the isomerization DIB tower (2), the top of the isomerization DIB tower (2) is connected with a dehydrogenation unit (5) through a refined isobutane outlet pipeline, the isomerization DIB tower (2) is connected with the butane isomerization device (3) through a normal butane outlet pipeline, and the isomerization DIB tower (2) is connected with the butane isomerization device (3) through a mixed butane inlet pipeline.
4. An energy efficient system for treating an isobutane dehydrogenation feed according to claim 3, wherein: the isomerism DIB tower (2) adopts a heat pump for rectification.
5. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the PSA hydrogen extraction unit (4) is connected with the butane isomerization device (3) through a first hydrogen inlet pipeline, and the PSA hydrogen extraction unit (4) is connected with the carbon four raw material pretreatment unit (1) through a second hydrogen inlet pipeline.
6. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the dehydrogenation unit (5) is connected with the PSA hydrogen extraction unit (4) through a crude hydrogen outlet pipeline.
7. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the deoxidization and hydrogenation unit comprises a CSP device (7) and a 0RU device (8), wherein the 0RU device (8) is connected with the CSP device (7) through a first circulating isobutane pipeline, and the CSP device (7) is connected with the isomerism DIB tower (2) through a second circulating isobutane pipeline.
8. An energy efficient system for processing isobutane dehydrogenation feed according to claim 7, wherein: the 0RU device (8) is connected with the MTBE unit (6) through a recycling regenerant outlet pipeline, and the MTBE unit (6) is connected with the 0RU device (8) through an isobutane outlet pipeline after the ether is discharged.
9. An energy efficient system for processing isobutane dehydrogenation feed according to claim 1, wherein: the MTBE unit (6) is provided with a methyl tertiary butyl ether outlet pipeline.
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| CN202321857718.3U CN220386515U (en) | 2023-07-14 | 2023-07-14 | Energy-saving system for treating isobutane dehydrogenation raw material |
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| CN202321857718.3U CN220386515U (en) | 2023-07-14 | 2023-07-14 | Energy-saving system for treating isobutane dehydrogenation raw material |
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