CN203725132U - Control system of reactor for preparing propylene from methanol - Google Patents
Control system of reactor for preparing propylene from methanol Download PDFInfo
- Publication number
- CN203725132U CN203725132U CN201320775704.7U CN201320775704U CN203725132U CN 203725132 U CN203725132 U CN 203725132U CN 201320775704 U CN201320775704 U CN 201320775704U CN 203725132 U CN203725132 U CN 203725132U
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- Prior art keywords
- reactor
- layer
- control system
- catalyst
- layers
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 48
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 title claims abstract description 20
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims abstract description 49
- 239000003054 catalyst Substances 0.000 claims abstract description 40
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 9
- 239000013505 freshwater Substances 0.000 claims description 16
- 238000007600 charging Methods 0.000 claims description 8
- 238000000889 atomisation Methods 0.000 claims description 7
- 238000010790 dilution Methods 0.000 claims description 7
- 239000012895 dilution Substances 0.000 claims description 7
- 238000004519 manufacturing process Methods 0.000 abstract description 9
- 239000007795 chemical reaction product Substances 0.000 abstract 1
- 238000000926 separation method Methods 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 description 13
- 238000000034 method Methods 0.000 description 6
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000009826 distribution Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 230000002463 transducing effect Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 239000012190 activator Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to an automatic control system. A control system of a reactor for preparing propylene from methanol is characterized in that hot dimethyl ether is fed from the top of the reactor; a reaction product is discharged from the bottom of the reactor and enters a separation unit; cold dimethyl ether enters each layer from the second catalyst layer to the bottom catalyst layer of the reactor, wherein each layer from the second catalyst layer to the bottom catalyst layer is provided with an FC (flow control) system for the cold dimethyl ether and a TC (temperature control) system; saturated diluted steam is fed from each layer from the second catalyst layer to the bottom catalyst layer of the reactor; a saturated diluted steam TC adjustment valve is arranged on the feeding pipe of each layer from the second catalyst layer to the bottom catalyst layer of the reactor and is connected with each TC system of each layer from the second catalyst layer to the bottom catalyst layer of the reactor. The control system is provided with a single loop control system; the single loop control system is simple in structure, low in investment, easily adjusted and put into operation and is particularly suitable for a controlled object with pure lag and a relatively small time constant, and can meet the requirement on the control of the production process.
Description
Technical field
The utility model relates to a kind of automatic control system, more particularly, relates to a kind of automatic control system of petrochemical industry.
Background technology
Along with the fast development of Coal Chemical Industry production technology, adopt the basic control system of DCS system as device.In technological reaction process, adopt Advanced Control Techniques, can bring considerable economic benefit to explained hereafter device.And, the optimization of device reaction Process Control System is more and more subject to the attention of each relevant enterprise.
Preparing propylene from methanol device is taking methyl alcohol as raw materials for production, through reaction and regeneration unit, washing unit, compression and pre-high unit, thermal release unit and cold separative element, the propylene refrigeration unit six part main technique production units of dividing, final production product is propylene, ethene, LPG and gasoline etc.Wherein, reaction adopts intercooled insulation fix bed reactor with regeneration unit, uses special zeolite catalyst, produces propylene by disproportionated reaction control reaction temperature.For preparing propylene from methanol device technique production control process, reaction is core technology with regeneration unit, the temperature control of reactor is directly involved in the service life of productivity of propylene and catalyst, and reaction and the procedure parameter in regeneration stage, must be controlled at the optimum state of art production process requirement.
Summary of the invention
The purpose of this utility model is to overcome the deficiencies in the prior art, and a kind of automatic control system of reactor is provided.
Preparing propylene from methanol reactor control system taking temperature control as core, its meaning is:
1, the overall reaction in preparing propylene from methanol reactor is strong exothermal reaction, must carry out centre cooling, so that Temperature Distribution is held in the temperature range of expectation.Centre is cooling to be completed by the each grade low-temp feed gas in centre.Preparing propylene from methanol reactor, can comprise 6 layers of beds, regulate the DME/ methanol vapor phase inlet amount of each beds, so that the Temperature Distribution in reactor and dimethyl ether concentration reach optimum, thereby ensure that reaction condition is consistent, obtain maximum propylene total recovery.
2, for ensureing that preparing propylene from methanol reaction is converted into the high selectivity of propylene, the operating temperature of beds must be controlled in certain temperature range, otherwise the carbon distribution speed of meeting accelerator activator, but also the hydrothermal stability of the serious test of meeting catalyst.
3, effectively control preparing propylene from methanol reaction temperature, in order to avoid fresh water (FW) and process steam that waste adds reach the object of saving the energy, reduce sewage load, reduce environmental pollution.
Cancel existing liquid phase feeding tandem regulation and control system, cancel existing cold dimethyl ether liquid phase feeding, improve preparing propylene from methanol reactor control system.
The control system of preparing propylene from methanol reactor, it is characterized in that, hot dimethyl ether is from reactor head charging, product from reactor bottom out, remove separative element, cold dimethyl ether enters each layer to the bottom of 2 layers of catalyst on reactor, is respectively equipped with the FC flow control system of cold dimethyl ether, the 2 layers of TC temperature control system of each layer to the bottom of catalyst on reactor; 2 layers of each layer of charging to the bottom of the catalyst of saturated dilution steam generation from reactor, 2 layers of catalyst on the reactor each layer of feed pipe to the bottom is provided with saturated dilution steam generation TC temperature control valve (TCV), and the each layer of upper TC temperature control system to the bottom is connected with 2 layers of catalyst on reactor respectively; Fresh water (FW) atomization gas enters the inlet tube of cold dimethyl ether, enters respectively each layer to the bottom of 2 layers of catalyst on reactor; Adopt branched armoured K-thermocouple to carry out temperature survey, branched armoured K-thermocouple inserts 2 layers of catalyst on reactor to each layer of the bottom; The inlet tube of cold dimethyl ether is respectively equipped with orifice plate, is connected with respectively differential pressure transmitter.
The utility model is provided with single loop control system 5 groups, is made up of basic link, contains measuring unit, transducing unit, adjuster and actuator.Single loop control system is simple in structure, and small investment is easy to adjust and put into operation, and can meet the control requirement of production process, is particularly useful for the pure hysteresis of controlled device and time constant less, load and the milder occasion of interference variations.
brief description of the drawings
Fig. 1 preparing propylene from methanol reactor control system sketch.
detailed description of the invention
Below in conjunction with accompanying drawing and specific embodiment, the utility model is made a further detailed description.
As shown in Figure 1,6 layers of hydrogen-catalyst reactor, hot dimethyl ether is from reactor head charging, product from reactor bottom out, remove separative element, cold dimethyl ether enters 2,3,4,5,6 layers of the catalyst of reactor, is respectively equipped with the FC flow control system of cold dimethyl ether, the TC temperature control system that the catalyst of reactor is 2,3,4,5,6 layers; Saturated dilution steam generation is from 2,3,4,5,6 layers of charging of catalyst of reactor, 2,3,4,5,6 layers of feed pipe of catalyst of reactor are provided with saturated dilution steam generation TC temperature control valve (TCV), are connected respectively with 2,3,4,5,6 layers of upper TC temperature control system of catalyst of reactor; Fresh water (FW) atomization gas enters the inlet tube of cold dimethyl ether, enters respectively 2,3,4,5,6 layers of the catalyst of reactor; Adopt branched armoured K-thermocouple to carry out temperature survey, branched armoured K-thermocouple inserts on 2,3,4,5,6 layers of the catalyst of reactor; The inlet tube of cold dimethyl ether is respectively equipped with orifice plate, is connected with respectively differential pressure transmitter; Hot dimethyl ether is 0.13～0.2MPaA from the pressure of reactor, hot dimethyl ether is from 475～485 DEG C of the head temperature of reactor, saturated dilution steam generation is from 165～175 DEG C of 2,3,4,5,6 layers of chargings of catalyst of reactor, and cold dimethyl ether is from 265～275 DEG C of 2,3,4,5,6 layers of chargings of catalyst of reactor; Fresh water (FW) atomization gas pipeline is communicated with cold dimethyl ether pipeline, fresh water (FW) atomization gas enters 2,3,4,5,6 layers of bottom of catalyst of reactor, by fresh water (FW) atomization gas, auxiliary each layer of temperature controlling reactor, prevent catalyst 2,3,4,5,6 each layers of temperature exceeding standard, can also on fresh water (FW) atomization gas pipeline, be provided with remote-controlled valve, by TA temperature indicating meter, realize straighforward operation.
Reactor described in the utility model has 6 layers of catalyst, is provided with 5 groups of single loop control systems, all belongs to basic control system, has measurement and transducing unit, adjuster and actuator.Single loop control system is simple in structure, and small investment is easy to adjust and put into operation, and can meet the control requirement of production process, is particularly useful for the pure hysteresis of controlled device and time constant less, load and the milder occasion of interference variations.
Claims (1)
1. the control system of a preparing propylene from methanol reactor, it is characterized in that, hot dimethyl ether is from reactor head charging, product from reactor bottom out, remove separative element, cold dimethyl ether enters each layer to the bottom of 2 layers of catalyst on reactor, is respectively equipped with the FC flow control system of cold dimethyl ether, the 2 layers of TC temperature control system of each layer to the bottom of catalyst on reactor; 2 layers of each layer of charging to the bottom of the catalyst of saturated dilution steam generation from reactor, 2 layers of catalyst on the reactor each layer of feed pipe to the bottom is provided with saturated dilution steam generation TC temperature control valve (TCV), and the each layer of upper TC temperature control system to the bottom is connected with 2 layers of catalyst on reactor respectively; Fresh water (FW) atomization gas enters the inlet tube of cold dimethyl ether, enters respectively each layer to the bottom of 2 layers of catalyst on reactor; Adopt branched armoured K-thermocouple to carry out temperature survey, branched armoured K-thermocouple inserts 2 layers of catalyst on reactor to each layer of the bottom; The inlet tube of cold dimethyl ether is respectively equipped with orifice plate, is connected with respectively differential pressure transmitter.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320775704.7U CN203725132U (en) | 2013-11-23 | 2013-11-23 | Control system of reactor for preparing propylene from methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320775704.7U CN203725132U (en) | 2013-11-23 | 2013-11-23 | Control system of reactor for preparing propylene from methanol |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203725132U true CN203725132U (en) | 2014-07-23 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201320775704.7U Expired - Lifetime CN203725132U (en) | 2013-11-23 | 2013-11-23 | Control system of reactor for preparing propylene from methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203725132U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103611477A (en) * | 2013-11-23 | 2014-03-05 | 中国石油集团东北炼化工程有限公司吉林设计院 | Control system of methanol to propylene reactor |
-
2013
- 2013-11-23 CN CN201320775704.7U patent/CN203725132U/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103611477A (en) * | 2013-11-23 | 2014-03-05 | 中国石油集团东北炼化工程有限公司吉林设计院 | Control system of methanol to propylene reactor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20201013 Address after: 132002 3-6 and 9-13 floors of Block A, Jihua Economic and Trade Center, Tongtan Road, Changyi District, Jilin Province Patentee after: PetroChina Jilin Chemical Engineering Co.,Ltd. Address before: Changyi District of Jilin city in Jilin province 132001 Tong Tan Road Jihua Trade Center building A Patentee before: JILIN DESIGNING INSTITUTE OF CNPC NORTHEAST REFINING & CHEMICAL ENGINEERING Co.,Ltd. |
|
| TR01 | Transfer of patent right | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140723 |
|
| CX01 | Expiry of patent term |