CN201087183Y - Technology device for comprehensive utilization of petrified waste - Google Patents
Technology device for comprehensive utilization of petrified waste Download PDFInfo
- Publication number
- CN201087183Y CN201087183Y CNU2007201158573U CN200720115857U CN201087183Y CN 201087183 Y CN201087183 Y CN 201087183Y CN U2007201158573 U CNU2007201158573 U CN U2007201158573U CN 200720115857 U CN200720115857 U CN 200720115857U CN 201087183 Y CN201087183 Y CN 201087183Y
- Authority
- CN
- China
- Prior art keywords
- tank
- tower
- successively
- cooling water
- sequence
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
- 239000002699 waste material Substances 0.000 title claims abstract description 10
- 238000005516 engineering process Methods 0.000 title abstract description 7
- 239000007788 liquid Substances 0.000 claims abstract description 26
- 238000000034 method Methods 0.000 claims abstract description 22
- 239000002283 diesel fuel Substances 0.000 claims abstract description 7
- 239000003502 gasoline Substances 0.000 claims abstract description 7
- 239000000295 fuel oil Substances 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims description 24
- 238000001816 cooling Methods 0.000 claims description 20
- 239000003381 stabilizer Substances 0.000 claims description 10
- 239000000203 mixture Substances 0.000 claims description 4
- 239000003921 oil Substances 0.000 abstract description 12
- 239000000446 fuel Substances 0.000 abstract description 4
- 238000010438 heat treatment Methods 0.000 abstract description 4
- 239000002994 raw material Substances 0.000 abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 239000000498 cooling water Substances 0.000 abstract 6
- 230000000087 stabilizing effect Effects 0.000 abstract 3
- 230000001131 transforming effect Effects 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 7
- 238000005336 cracking Methods 0.000 description 4
- 238000006555 catalytic reaction Methods 0.000 description 3
- 235000019628 coolness Nutrition 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000003915 liquefied petroleum gas Substances 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The utility model relates to a petrified wastes comprehensive utilization technology device. The investment of the current process equipment is great, and the transforming quality is not high. The petrified wastes comprehensive utilization technology device adopts a structure that a raw material tank (1) is connected in sequence with a raw material pump (2), a first heating furnace (3), a first reacting device (4), a second heating furnace (5), a second reacting device (6), a fractionating tower (7), a second cooling water tank (9), an oil water separating tank (14), a compressor (17), a fourth cooling water tank (18), a gas liquid separating tank (19), and a stabilizing tower (16), wherein, one end of the stabilizing tower is connected in sequence with a sixth cooling water tank (22), a gas liquid separating tank A (23) and a liquefied gas tank (24), and the other end is connected in sequence with a fifth cooling water tank (20) and a gasoline tank (21), the fractionating tower is connected in sequence with a first cooling water tank (8) and a heavy oil tank (10), the stabilizing tower is connected in sequence with a stripping tower (11), a third cooling water tank (12) and a diesel oil tank (13), and the oil water separating tank is connected with a gasoline pump (15). The product is adopted as fuel transforming equipment.
Description
Technical field:
The utility model relates to a kind of fuel conversion process equipment, is specifically related to a kind of petrochemical industry waste ' s reclamation technique device.
Background technology:
At present, in fuel conversion process equipment is used, mainly adopt non-hydro-dewaxing to make zero pour become liquefied petroleum gas (LPG) with fixed attention through catalysis at the 30-40 ℃ of higher oil of the normal pressure content of wax three-way, the decompression two wires.This technology expends a large amount of hydrogen, can only transform 90# gasoline and the diesel oil below-10 ℃.Obviously, cost of investment is big, working cost is high, the operational condition High Temperature High Pressure, to transform of low quality be its outstanding defective and deficiency.
Summary of the invention:
The purpose of this utility model provides a kind of petrochemical industry waste ' s reclamation technique device, and cost of investment is less, consumption hydrogen is few, working pressure is low, good stability.
Above-mentioned purpose realizes by following technical scheme:
Petrochemical industry waste ' s reclamation technique device, its composition comprises: head tank, described head tank connects feedstock pump successively, a process furnace, a reactor, No. two process furnace, No. two reactors, separation column, No. two cooling troughes, gun barrel, compressor, No. four cold rinse banks, vapor-liquid separation tank, stabilizer tower, described stabilizer tower one end connects cooling trough successively No. six, vapor-liquid separation tank A, liquid gas storage tank, the other end connects cold rinse bank successively No. five, gasoline tank, described separation column connects cooling trough successively No. one, heavy oil tank, described separation column connects stripping tower successively, three cooling troughes, diesel fuel tank, described gun barrel connects petrol-feed pump.
The beneficial effects of the utility model:
Raw material of the present utility model (slop wax oil) is extracted out through pump, send into the process furnace heating after the product heat exchange, slop wax oil is reached about temperature of reaction (450 ℃), material flows out from the first pipe group after heating, entering second reactor contacts with reaction medium, data cracking building-up reactions takes place, reenter the process furnace second pipe group through the material of initial reaction and reheat temperature of reaction (450 ℃), enter second reactor then and finish catalytic reaction process, substantially, be converted into the finished fluid fluid fuel through the material after twice catalysis, through heat exchange, cooling, enter basin after the washing.This device has that working cost is low, technology is fairly simple, the recovery time is short, exquisiteness is effective, stability is strong, broad-spectrum characteristics, and good product quality.
Description of drawings:
Accompanying drawing 1 is an apparatus and process schema of the present utility model.
Embodiment:
Embodiment 1:
Petrochemical industry waste ' s reclamation technique device, its composition comprises: head tank 1, described head tank connects feedstock pump 2 successively, a process furnace 3, a reactor 4, No. two process furnace 5, No. two reactors 6, separation column 7, No. two cooling troughes 9, gun barrel 14, compressor 17, No. four cold rinse banks 18, vapor-liquid separation tank 19, stabilizer tower 16, described stabilizer tower one end connects cooling trough 22 successively No. six, vapor-liquid separation tank A23, liquid gas storage tank 24, the other end connects cold rinse bank 20 successively No. five, gasoline tank 21, described separation column connects cooling trough 8 successively No. one, heavy oil tank 10, described separation column connects stripping tower 11 successively, three cooling troughes 12, diesel fuel tank 13, described gun barrel connects petrol-feed pump 15.
Adopt static catalytic cracking technology to reach refining effect in a described reactor and No. two reactors to the petrochemical industry waste.
Below in conjunction with accompanying drawing the utility model embodiment is described in detail: raw material forwards feedstock pump 2 to by head tank 1, is transported to a process furnace 3 and heats.In boiler tube, form gas-oil mixture matter and be transferred to reactor 4 No. one.Oil gas carries out scission reaction after entering into reactor under the effect of catalyzer, form the vapour-liquid body.Because the minimizing of heat, so medium is transferred to No. two process furnace 5 once more, improve once more after the temperature, be transferred to reactor 6 No. two, under the effect of catalyzer, will not decompose a large amount of oil gas of the further drastic cracking cracking generation of cracking molecule and be transferred to separation column 7 feed zones.After oil gas entered in the tower, vapour phase continued to rise, and liquid is fallen at the bottom of the tower, after heavy oil is extracted out by pump at the bottom of the tower, through being sent to finished product jar (heavy oil tank 10) after No. two cooling trough 9 coolings.
After the interior vapor-liquid separation of separation column, gas continues in the uphill process, carry out flowing into stripping tower 11 after liquid that cold and hot clearing house produces is fallen tower middle part oil header with the liquid of interior whereabouts, be diesel oil at the bottom of liquid is fallen tower afterwards through stripping, be pumped out after 12 coolings of three cooling troughes and be transferred to product tank (diesel fuel tank 13).
The oil gas that the separation column top produces is transferred to after a cooling trough 8 cools off, the vapour-liquid that forms flow into gun barrel 14, water is cut after carrying out oily water separation, oil (raw gasline) is extracted out parts by petrol-feed pump 15 and is done trim the top of column (about 450 ℃ of control top temperature), and another part passes on stabilizer tower 16 and carries out desorb.The gas of separation column gun barrel is transferred to the compressed cold rinse bank 18 that is transferred to No. four afterwards of compressor 17 one-levels inlet, cool off and be transferred to vapor-liquid separation tank 19 then again, liquid is sent back in the stabilizer tower, gas be transferred to liquid (liquefied gas) that compressor secondary inlet is compressed generation once more be transferred in the stabilizer tower intercourse with raw gasline vapour-liquid in tower after liquid fall and be sent to finished product jar (gasoline tank 21) through No. five cold rinse banks 20 coolings after being pumped out at the bottom of the tower.
Vapour phase medium in the stabilizer tower is transferred to No. six cooling troughes 22 through the cat head outflow and cools off, and formation vapour-liquid material flow into vapor-liquid separation tank A23 and carries out vapor-liquid separation, and vapour phase is that net gas is directly delivered to finished product jar (liquid gas storage tank 24).
Claims (1)
1. petrochemical industry waste ' s reclamation technique device, its composition comprises: head tank, it is characterized in that: described head tank connects feedstock pump successively, a process furnace, a reactor, No. two process furnace, No. two reactors, separation column, No. two cooling troughes, gun barrel, compressor, No. four cold rinse banks, vapor-liquid separation tank, stabilizer tower, described stabilizer tower one end connects cooling trough successively No. six, vapor-liquid separation tank A, liquid gas storage tank, the other end connects cold rinse bank successively No. five, gasoline tank, described separation column connects cooling trough successively No. one, heavy oil tank, described separation column connects stripping tower successively, three cooling troughes, diesel fuel tank, described gun barrel connects petrol-feed pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201158573U CN201087183Y (en) | 2007-03-29 | 2007-03-29 | Technology device for comprehensive utilization of petrified waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201158573U CN201087183Y (en) | 2007-03-29 | 2007-03-29 | Technology device for comprehensive utilization of petrified waste |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201087183Y true CN201087183Y (en) | 2008-07-16 |
Family
ID=39634777
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007201158573U Expired - Fee Related CN201087183Y (en) | 2007-03-29 | 2007-03-29 | Technology device for comprehensive utilization of petrified waste |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201087183Y (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101798526B (en) * | 2009-02-09 | 2013-03-27 | 新疆现代石油化工股份有限公司 | Non-hydrogen dewaxing depressurizing distillation process and device |
-
2007
- 2007-03-29 CN CNU2007201158573U patent/CN201087183Y/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101798526B (en) * | 2009-02-09 | 2013-03-27 | 新疆现代石油化工股份有限公司 | Non-hydrogen dewaxing depressurizing distillation process and device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP3341578B1 (en) | Recovery and re-use of waste energy in industrial facilities | |
| CN103232312A (en) | Device and process for preparing isobutylene by dehydrogenating isobutane | |
| CN205740904U (en) | Petroleum naphtha hydrogenation refines low pressure deoxidation and the system of charging heat exchange optimization | |
| CN104177214B (en) | A kind of catalytic cracking rich gas and methanol to olefins reaction product composite liberation method | |
| CN101559311A (en) | Step recovery method for centralizing refinery gas | |
| CN102659076B (en) | Method for co-production of various chemical products from natural gas, coal and petroleum | |
| CN101244970A (en) | Apparatus and technique for producing ethylene with ethyl alcohol | |
| CN110669543A (en) | Device and method for directly preparing gasoline by carbon dioxide hydrogenation | |
| CN100516008C (en) | Process for cracking isobutene by methyl-tert-butyl ether | |
| CN102718617B (en) | System and method for refining isobutane | |
| CN201087183Y (en) | Technology device for comprehensive utilization of petrified waste | |
| CN203333598U (en) | Processing device for modifying light hydrocarbons | |
| CN100473712C (en) | Technical flow of hydrogenation of gasoline through catalytic cracking full distillate | |
| CN115785999A (en) | Method and system for producing gasoline and diesel oil from condensate oil | |
| CN210595940U (en) | Heat conduction oil processing device | |
| CN207749076U (en) | A kind of refinery product's upgrading synergy and hydrogen recovery system | |
| CN205061982U (en) | Methyl alcohol system lighter hydrocarbons process systems that energy integration utilized | |
| CN109022031A (en) | Reduce the delayed coking method and processing of heavy oil method of sewage discharge | |
| CN109181766A (en) | A kind of modified light aromatic hydrocarbons hydrogenation plant and its operating method | |
| CN217041932U (en) | Exhaust treatment device for oil depot | |
| CN218089443U (en) | Rectification and removal device for dimethyl ether in carbon-tetrad hydrocarbons | |
| CN110295059B (en) | Catalytic cracking process and system | |
| CN104419436B (en) | A kind of direct coal liquefaction process using poor oil | |
| WO2020062198A1 (en) | Residue oil hydrogenation production system | |
| CN203782054U (en) | Methanol-to-olefin system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: HARBIN JINWU PETROCHEMICAL CO., LTD. Free format text: FORMER OWNER: YANG DONGJUN Effective date: 20120524 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 150001 HARBIN, HEILONGJIANG PROVINCE TO: 150020 HARBIN, HEILONGJIANG PROVINCE |
|
| TR01 | Transfer of patent right |
Effective date of registration: 20120524 Address after: 150020, Heilongjiang, Harbin Province town solidarity village dividends Village Patentee after: Harbin Jin Wu Formosa Petrochemical Co Address before: 150001 Heilongjiang city of Harbin province Daoli District West nine Street No. 15 building 16 room 5 Londian Patentee before: Yang Dongjun |
|
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080716 Termination date: 20160329 |