CN214064860U - Isothermal transformation byproduct steam recycling heat network system - Google Patents
Isothermal transformation byproduct steam recycling heat network system Download PDFInfo
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- CN214064860U CN214064860U CN202023140902.5U CN202023140902U CN214064860U CN 214064860 U CN214064860 U CN 214064860U CN 202023140902 U CN202023140902 U CN 202023140902U CN 214064860 U CN214064860 U CN 214064860U
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- steam
- heater
- pipe network
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- pressure
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- 239000006227 byproduct Substances 0.000 title claims abstract description 22
- 230000009466 transformation Effects 0.000 title claims abstract description 19
- 238000004064 recycling Methods 0.000 title claims abstract description 11
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 20
- 239000000571 coke Substances 0.000 claims abstract description 10
- 238000010438 heat treatment Methods 0.000 claims abstract description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 36
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 30
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 230000008929 regeneration Effects 0.000 abstract description 28
- 238000011069 regeneration method Methods 0.000 abstract description 28
- 238000000034 method Methods 0.000 abstract description 2
- 238000004134 energy conservation Methods 0.000 abstract 1
- 238000005485 electric heating Methods 0.000 description 7
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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- 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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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a coke oven gas demercuration hydrogenation field, concretely relates to isothermal transformation byproduct steam recycling heat network system, including reciprocating engine, steam heater and pre-hydrogenation converter, coke oven gas is sent to the pre-hydrogenation converter after heating through steam heater, still includes transformation medium pressure gas bag, debenzolization system regeneration gas heater, the decalcification system regeneration gas heater, medium pressure steam pipe network and low pressure steam pipe network, transformation medium pressure gas bag is connected with steam heater and medium pressure steam pipe network respectively through the pipeline, debenzolization system regeneration gas heater and the decalcification system regeneration gas heater are connected to medium pressure steam pipe network respectively through the pipeline, steam heater, debenzolization system regeneration gas heater and the decalcification system regeneration gas heater still are connected with steam condensate tank respectively, the utility model relates to an ingenious, rational in infrastructure, can effectively solve the potential safety hazard in the coke oven gas demercuration hydrogenation process in the prior art, the purposes of energy conservation and emission reduction are achieved, and the method is suitable for wide popularization and application.
Description
Technical Field
The utility model relates to a coke oven gas demercuration hydrogenation field, concretely relates to isothermal transformation byproduct steam recycles heat supply network system.
Background
The method comprises the steps that coke-oven gas from a reciprocating compressor enters an oil absorption groove to remove gas mechanical oil, then enters a demercuration groove to remove mercury, then enters a coke-oven gas heater and a primary hydrogenation converter, the coke-oven gas is heated to 180 ℃ by the coke-oven gas heater and then enters the primary hydrogenation converter, the traditional coke-oven gas demercuration hydrogenation uses an electric heating furnace to heat coke-oven gas of about 4.0Mpa sent by a reciprocating machine to 180 ℃, so that the coke-oven gas reaches a conversion temperature when entering a pre-hydrogenation converter, and because the electric heating furnace has unsafe factors, the technical problems need to be solved and improved.
Therefore, it is necessary to solve the above-mentioned technical problems.
SUMMERY OF THE UTILITY MODEL
In order to solve the technical problem, the utility model provides an isothermal transformation byproduct steam recycles heat supply network system can effectively solve the problem of the production potential safety hazard in the coke-oven gas heating process, the utility model discloses a technical scheme as follows:
a heat network system for recycling isothermal shift byproduct steam is used for demercuration and hydrogenation of coke-oven gas and comprises a reciprocating engine, a steam heater and a pre-hydrogenation converter, wherein the coke-oven gas is heated by the steam heater and then sent to the pre-hydrogenation converter, the heat network system also comprises a shift medium-pressure gas bag, a debenzolization system regeneration gas heater, a naphthalene removal system regeneration gas heater, a medium-pressure steam pipe network and a low-pressure steam pipe network, the shift medium-pressure gas bag is respectively connected with the steam heater and the medium-pressure steam pipe network through pipelines, medium-pressure steam of shift byproducts is arranged in the gas bag, one part of the steam enters the steam heater, the other part of the steam enters the medium-pressure steam pipe network, the benzene removal system regeneration gas heater and the naphthalene removal system regeneration gas heater are respectively connected to the medium-pressure steam pipe network through pipelines, the steam of the medium-pressure steam pipe network is used as a heating source, and the steam heater, the benzene removal system regeneration gas heater and the naphthalene removal system regeneration gas heater are respectively connected with a steam condensate tank, wherein the steam condensate tank that links to each other with steam heater still is connected with middling pressure steam pipe network, send the steam of noncondensation to middling pressure steam pipe network, and the steam condensate tank that links to each other with benzene removal system regeneration gas heater, naphthalene removal system regeneration gas heater then links to each other with low pressure steam pipe network, and the condensate in every steam condensate tank then retrieves respectively to the condensate pipe network.
Further, the steam contained in the shift conversion medium-pressure gas bag is the shift conversion by-product medium-pressure steam with the pressure of 4.0-5.0 MPa.
Further, the medium pressure steam in the medium pressure steam pipe network is 2.5 Mpa.
Further, the low-pressure steam in the low-pressure steam pipe network is 0.5 Mpa.
Further, the coke oven gas in the reciprocating machine is 4.0Mpa, and is heated to 180 ℃ by a steam heater.
Compared with the prior art, the utility model discloses the beneficial effect who has does:
1. the utility model discloses an increase and set up steam heater and condensate tank and replace electric heating furnace, reduce the potential safety hazard that exists in the production process, guaranteed production safety effectively.
2. The utility model discloses in through rationally setting up isothermal transformation by-product steam and recycling heat network, carry out complete recycle to isothermal transformation by-product's 5.0Mpa steam heat, reached energy saving and emission reduction's purpose effectively, reduced manufacturing cost.
3. The utility model discloses in through the reasonable setting of steam heat network of recycling, follow-up benzene system regeneration gas heater and the heat source problem of taking off naphthalene system regeneration gas heater of taking off in the heating of coke-oven gas has still been solved effectively, has further improved energy utilization.
To sum up, the utility model relates to an ingenious, rational in infrastructure, can effectively solve the potential safety hazard problem among the prior art coke-oven gas demercuration hydrogenation process, reach energy saving and emission reduction's purpose, be fit for extensively using widely.
Drawings
FIG. 1 is a block diagram of the connection structure of the present invention;
Detailed Description
The technical solutions in the embodiments of the present invention are described below clearly and completely, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Referring to fig. 1, the utility model provides a heat supply network system is recycled to isothermal transformation byproduct steam for coke-oven gas demercuration hydrogenation, including reciprocating engine, steam heater and pre-hydrogenation converter, coke-oven gas sends to pre-hydrogenation converter after passing through steam heater heating, still includes transformation medium pressure gas package, debenzolization system regeneration gas heater, the system regeneration gas heater of naphthalene removal, medium pressure steam pipe network and low pressure steam pipe network, the transformation medium pressure gas package is connected with steam heater and medium pressure steam pipe network respectively through the pipeline, is the medium pressure steam of transformation byproduct in the gas package, and partly steam gets into steam heater, and another part gets into medium pressure steam pipe network, debenzolization system regeneration gas heater and the system regeneration gas heater of naphthalene removal are connected to medium pressure steam pipe network through the pipeline respectively, regard as the heating source by the steam of medium pressure steam pipe network, steam heater, The device comprises a benzene removal system regeneration gas heater, a naphthalene removal system regeneration gas heater, a steam condensate tank, a medium-pressure steam pipe network, a low-pressure steam pipe network, a benzene removal system regeneration gas heater, a naphthalene removal system regeneration gas heater, a low-pressure steam pipe network and a condensate tank, wherein the benzene removal system regeneration gas heater and the naphthalene removal system regeneration gas heater are respectively connected with the steam condensate tank, the steam condensate tank connected with the steam heater is also connected with the medium-pressure steam pipe network, uncondensed steam is sent to the medium-pressure steam pipe network, the steam condensate tank connected with the benzene removal system regeneration gas heater and the naphthalene removal system regeneration gas heater is connected with the low-pressure steam pipe network, and condensate in each steam condensate tank is respectively recovered to the condensate pipe network.
The steam contained in the shift medium-pressure gas bag is the shift byproduct medium-pressure steam with the pressure of 4.0-5.0 Mpa.
And the medium-pressure steam in the medium-pressure steam pipe network is 2.5 Mpa.
The low-pressure steam in the low-pressure steam pipe network is 0.5 Mpa.
The coke oven gas in the reciprocating machine is 4.0Mpa, and is heated to 180 ℃ by a steam heater.
The utility model relates to a principle does:
the demercuration and hydrogenation of the coke-oven gas uses an electric heating furnace to heat the coke-oven gas which is sent by a reciprocating engine and has the pressure of about 4.0Mpa to 180 ℃, so that the coke-oven gas reaches the conversion temperature when entering a pre-hydrogenation converter, and because the electric heating furnace brings unsafe factors, a steam heater with the pressure of 112m2 and a condensate tank are added in a workshop to replace the electric heating furnace. Steam used by the steam heater is medium-pressure steam which is a transformation byproduct and is reduced in pressure from 5.0MPa to 2.5MPa, condensate out of the steam heater enters a steam condensing tank to be flashed, the condensate is recycled to a condensate pipe network, uncondensed steam is recycled to a 2.5MPa steam pipe network, regenerated gas in a temperature swing adsorption section is heated again, the steam and the condensate out of the regenerated gas heater are flashed again through a condensate vaporizing tank, the uncondensed steam is recycled to the 0.5MPa steam pipe network, and the rest condensate is recycled to the condensate pipe network. Through the transformation: the byproduct steam heat of 5.0Mpa is completely recycled, thereby achieving the purpose of energy saving. The steam heater replaces an electric heating furnace, so that potential safety hazards in the production process are reduced.
The above description has been made in detail only for the preferred embodiment of the present invention, but the present invention is not limited to the above embodiment, and various changes can be made without departing from the spirit of the present invention within the knowledge scope of those skilled in the art, and all such changes are intended to be encompassed by the present invention.
Claims (5)
1. A heat network system for recycling isothermal transformation byproduct steam is used for demercuration and hydrogenation of coke oven gas, and is characterized in that: the coke oven gas is heated by the steam heater and then sent to the pre-hydrogenation converter, the coke oven gas further comprises a transformation medium-pressure gas bag, a benzene removal system regenerated gas heater, a naphthalene removal system regenerated gas heater, a medium-pressure steam pipe network and a low-pressure steam pipe network, the transformation medium-pressure gas bag is respectively connected with the steam heater and the medium-pressure steam pipe network through pipelines, medium-pressure steam of transformation byproducts is arranged in the gas bag, one part of the steam enters the steam heater, the other part of the steam enters the medium-pressure steam pipe network, the benzene removal system regenerated gas heater and the naphthalene removal system regenerated gas heater are respectively connected to the medium-pressure steam pipe network through pipelines, the steam of the medium-pressure steam pipe network is used as a heating source, the steam heater, the benzene removal system regenerated gas heater and the naphthalene removal system regenerated gas heater are respectively connected with steam condensate tanks, wherein the steam condensate tanks connected with the steam heater are also connected with the medium-pressure steam pipe network, and (3) sending uncondensed steam to a medium-pressure steam pipe network, connecting a steam condensate tank connected with a benzene removal system regenerated gas heater and a naphthalene removal system regenerated gas heater with a low-pressure steam pipe network, and respectively recovering condensate in each steam condensate tank to a condensate pipe network.
2. The isothermal shift conversion byproduct steam recycling heat network system according to claim 1, wherein: the steam contained in the shift medium-pressure gas bag is the shift byproduct medium-pressure steam with the pressure of 4.0-5.0 Mpa.
3. The isothermal shift conversion byproduct steam recycling heat network system according to claim 1, wherein: and the medium-pressure steam in the medium-pressure steam pipe network is 2.5 Mpa.
4. The isothermal shift conversion byproduct steam recycling heat network system according to claim 1, wherein: the low-pressure steam in the low-pressure steam pipe network is 0.5 Mpa.
5. The isothermal shift conversion byproduct steam recycling heat network system according to claim 1, wherein: the coke oven gas in the reciprocating machine is 4.0Mpa, and is heated to 180 ℃ by a steam heater.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023140902.5U CN214064860U (en) | 2020-12-23 | 2020-12-23 | Isothermal transformation byproduct steam recycling heat network system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202023140902.5U CN214064860U (en) | 2020-12-23 | 2020-12-23 | Isothermal transformation byproduct steam recycling heat network system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN214064860U true CN214064860U (en) | 2021-08-27 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202023140902.5U Expired - Fee Related CN214064860U (en) | 2020-12-23 | 2020-12-23 | Isothermal transformation byproduct steam recycling heat network system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN214064860U (en) |
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2020
- 2020-12-23 CN CN202023140902.5U patent/CN214064860U/en not_active Expired - Fee Related
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|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20210827 |