CN109971513A - Multistage Cooling Technology and Device of Coke Oven Waste Gas - Google Patents
Multistage Cooling Technology and Device of Coke Oven Waste Gas Download PDFInfo
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- CN109971513A CN109971513A CN201910228039.1A CN201910228039A CN109971513A CN 109971513 A CN109971513 A CN 109971513A CN 201910228039 A CN201910228039 A CN 201910228039A CN 109971513 A CN109971513 A CN 109971513A
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- 239000002912 waste gas Substances 0.000 title claims abstract description 90
- 238000001816 cooling Methods 0.000 title claims abstract description 33
- 239000000571 coke Substances 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 230000008569 process Effects 0.000 claims abstract description 22
- 239000007789 gas Substances 0.000 claims abstract description 21
- 238000000926 separation method Methods 0.000 claims abstract description 14
- 238000003763 carbonization Methods 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 9
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 4
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 claims description 4
- 239000010426 asphalt Substances 0.000 claims description 3
- 238000010025 steaming Methods 0.000 claims description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 abstract description 6
- 238000011084 recovery Methods 0.000 abstract description 4
- 230000009286 beneficial effect Effects 0.000 abstract description 2
- 238000009833 condensation Methods 0.000 abstract description 2
- 230000005494 condensation Effects 0.000 abstract description 2
- 238000000605 extraction Methods 0.000 abstract 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 10
- 238000004939 coking Methods 0.000 description 7
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 5
- 229910021529 ammonia Inorganic materials 0.000 description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 238000011112 process operation Methods 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000000844 transformation Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B27/00—Arrangements for withdrawal of the distillation gases
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
-
- 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
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Materials Engineering (AREA)
- Industrial Gases (AREA)
Abstract
本发明涉及焦炉高温荒煤气冷却、焦油馏分采取及余热回收技术领域，具体涉及一种焦炉荒煤气的多级冷却装置及其工艺。本发明的技术方案为：焦炉煤气离开焦炉，通过上升管后依次通过一级换热器、一级闪蒸罐、二级换热器、二级闪蒸罐、三级换热器、三级闪蒸罐，最后进入初冷器，通过调节除氧水的流量来控制荒煤气的冷却后温度。本发明的有益效果在于：通过对焦炉荒煤气采用多段分级冷却，实现荒煤气由650～750℃冷却到80～90℃，并发生高、中和低压蒸汽，同时分离焦油高温馏分、中温馏分和轻油馏分。本发明有以下优势：（1）充分回收了荒煤气余热；（2）实现了荒煤气中馏分的粗分离；（3）多级冷凝温度可调控。The invention relates to the technical field of coke oven high-temperature waste gas cooling, tar fraction extraction and waste heat recovery, in particular to a multi-stage cooling device for coke oven waste gas and a process thereof. The technical scheme of the present invention is as follows: the coke oven gas leaves the coke oven, passes through the riser pipe, passes through the primary heat exchanger, the primary flash tank, the secondary heat exchanger, the secondary flash tank, the tertiary heat exchanger, The three-stage flash tank finally enters the primary cooler, and the cooling temperature of the waste gas is controlled by adjusting the flow rate of the deoxygenated water. The beneficial effect of the invention is that: by adopting multi-stage grading cooling of coke oven waste gas, the waste gas can be cooled from 650-750 DEG C to 80-90 DEG C, and high, medium and low pressure steam is generated, and high-temperature fraction and medium-temperature fraction of tar are separated at the same time. and light oil fractions. The invention has the following advantages: (1) the waste heat of the waste gas is fully recovered; (2) the rough separation of the distillate in the waste gas is realized; (3) the multi-stage condensation temperature can be adjusted.
Description
技术领域technical field
本发明涉及焦炉高温荒煤气冷却、焦油馏分分离及余热回收技术领域，具体涉及一种焦炉荒煤气的多级冷却工艺与装置。The invention relates to the technical field of coke oven high-temperature waste gas cooling, tar fraction separation and waste heat recovery, in particular to a multi-stage cooling process and device for coke oven waste gas.
背景技术Background technique
炼焦工业是伴随着钢铁企业的发展而发展的，也是钢铁工业的基础产业之一，同时焦化工业也是耗能大户，其中炼焦过程加热消耗约占煤气产量的45％～50％，因此焦化行业也是节能减排的重要行业。煤在炼焦时除了有75％左右变成焦炭外，还有约25％生成各种化学产品及煤气。回收这些化学产品对综合利用煤炭资源和经济建设有着重要的意义。The coking industry has developed along with the development of iron and steel enterprises, and it is also one of the basic industries of the iron and steel industry. At the same time, the coking industry is also a large energy consumer. Among them, the heating consumption of the coking process accounts for about 45% to 50% of the gas output. Therefore, the coking industry is also An important industry for energy conservation and emission reduction. When coal is coking, about 75% becomes coke, and about 25% generates various chemical products and gas. The recovery of these chemical products is of great significance to the comprehensive utilization of coal resources and economic construction.
现有的焦炉荒煤气冷却工艺中通常的做法是：将来自焦炉炭化室的650～750℃荒煤气，经焦炉上升管，后进入集气槽。在集气槽内喷洒循环氨水与荒煤气直接接触冷却，靠循环氨水大量汽化，使荒煤气急剧降温至80～90℃，然后在初冷器中冷却到25～35℃后送至后续工序。此过程大量的热能未被利用，且需要大量的循环氨水。The usual practice in the existing coke oven waste gas cooling process is: the 650-750°C waste gas from the coke oven carbonization chamber is passed through the coke oven riser pipe and then enters the gas collecting tank. Spray circulating ammonia water in the gas collecting tank to directly contact and cool the waste gas, and the waste gas is rapidly cooled to 80-90 ℃ by the vaporization of the circulating ammonia water, and then cooled to 25-35 ℃ in the primary cooler and sent to the subsequent process. A large amount of thermal energy is not utilized in this process, and a large amount of circulating ammonia water is required.
发明内容SUMMARY OF THE INVENTION
本发明旨在提供一种焦炉荒煤气的多级冷却工艺及装置，同步实现焦炉荒煤气冷却、余热回收和焦油馏分分离。The invention aims to provide a multi-stage cooling process and device for coke oven waste gas, which simultaneously realizes coke oven waste gas cooling, waste heat recovery and tar fraction separation.
本发明为解决上述提出的问题所采用的技术方案为：The technical scheme adopted by the present invention to solve the above-mentioned problems is:
一种焦炉荒煤气的多级冷却装置，主要包括焦炉炭化室、一级换热器、一级闪蒸罐、二级换热器、二级闪蒸罐、三级换热器、三级闪蒸罐、初冷器，其中，焦炉炭化室的荒煤气出口与一级换热器的荒煤气入口相连，一级换热器的荒煤气出口与一级闪蒸罐的进料口相连，一级闪蒸罐顶部与二级换热器的荒煤气入口相连，二级换热器的荒煤气出口与二级闪蒸罐的进料口相连，二级闪蒸罐顶部与三级换热器的荒煤气入口相连，三级换热器的荒煤气出口与三级闪蒸罐的进料口相连，三级闪蒸罐顶部与初冷器的入口相连。A multi-stage cooling device for coke oven waste gas mainly includes a coke oven carbonization chamber, a primary heat exchanger, a primary flash tank, a secondary heat exchanger, a secondary flash tank, a tertiary heat exchanger, a Stage flash tank and primary cooler, wherein the waste gas outlet of the coke oven carbonization chamber is connected to the waste gas inlet of the primary heat exchanger, and the waste gas outlet of the primary heat exchanger is connected to the feed inlet of the primary flash tank Connected, the top of the primary flash tank is connected to the raw gas inlet of the secondary heat exchanger, the waste gas outlet of the secondary heat exchanger is connected to the feed port of the secondary flash tank, and the top of the secondary flash tank is connected to the third-level flash tank. The waste gas inlet of the heat exchanger is connected, the waste gas outlet of the tertiary heat exchanger is connected with the feed inlet of the tertiary flash tank, and the top of the tertiary flash tank is connected with the inlet of the primary cooler.
进一步地，一级换热器、二级换热器、三级换热器上均分别开设有除氧水的入口以及蒸汽出口。Further, the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger are respectively provided with an inlet of deoxygenated water and a steam outlet.
进一步地，一级换热器、二级换热器、三级换热器的除氧水入口处均安装有除氧水流量控制阀。更进一步地，还包括三个控制流量调节的温度显示控制器，每个控制流量调节的温度显示控制器的两端分别连接同一个换热器除氧水入口处的除氧水流量控制阀和荒煤气出口。Further, a deoxygenated water flow control valve is installed at the deoxygenated water inlets of the primary heat exchanger, the secondary heat exchanger and the tertiary heat exchanger. Further, it also includes three temperature display controllers for controlling flow regulation, and the two ends of each temperature display controller for controlling flow regulation are respectively connected to the deaerated water flow control valve and the deaeration water flow control valve at the same heat exchanger deaeration water inlet. Barren gas outlet.
本发明还提供一种焦炉荒煤气的多级冷却工艺，是将荒煤气由650～750℃冷却到80～90℃，并回收煤气余热产生高、中和低压蒸汽，同时分离焦油高温、中温和低温馏分，具体操作步骤如下：The invention also provides a multi-stage cooling process for coke oven waste gas, which is to cool the waste gas from 650-750 DEG C to 80-90 DEG C, recover the waste heat of the gas to generate high, medium and low pressure steam, and simultaneously separate the tar high temperature, medium and low pressure steam. Mild and low temperature fraction, the specific operation steps are as follows:
(1)来自焦炉炭化室的650～750℃高温荒煤气，先经一级换热器冷却，荒煤气温度降至275～285℃后，再经过一级闪蒸罐进行气液分离，底部分离出高温馏分，顶部分离出的荒煤气通往二级换热器；(1) The high-temperature waste gas at 650-750°C from the coke oven carbonization chamber is first cooled by the primary heat exchanger. After the temperature of the waste gas is reduced to 275-285°C, the gas-liquid separation is carried out through the primary flash tank. The high temperature fraction is separated, and the waste gas separated at the top is sent to the secondary heat exchanger;
(2)来自一级闪蒸罐的荒煤气经过二级换热器冷却，荒煤气温度降至165～175℃后，再经过二级闪蒸罐进行气液分离，底部分离出中温馏分，顶部分离出的荒煤气通往三级换热器；(2) The waste gas from the primary flash tank is cooled by the secondary heat exchanger, and after the temperature of the waste gas drops to 165-175 °C, the gas-liquid separation is carried out through the secondary flash tank, and the middle temperature fraction is separated at the bottom and the top The separated waste gas is sent to the three-stage heat exchanger;
(3)来自二级闪蒸罐的荒煤气经过三级换热器冷却，荒煤气温度降至80～90℃后，再经过三级闪蒸罐进行气液分离，底部分离出低温馏分，顶部分离出的荒煤气通往初冷器冷却，冷却至25～35℃后送至后续工序。(3) The waste gas from the second-stage flash tank is cooled by the third-stage heat exchanger. After the temperature of the waste gas drops to 80-90 °C, the gas-liquid separation is carried out through the third-stage flash tank, and the low-temperature fraction is separated at the bottom and the top The separated waste gas is sent to the primary cooler for cooling, and then sent to the subsequent process after cooling to 25-35 °C.
按上述方案，在一级换热器、二级换热器、三级换热器中分别通过3.5MPa、1.0MPa和0.35MPa的除氧水发生蒸汽以回收荒煤气的热量。According to the above scheme, steam is generated through deoxygenated water of 3.5MPa, 1.0MPa and 0.35MPa in the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger respectively to recover the heat of the waste gas.
按上述方案，通过除氧水通入分别通入一级换热器、二级换热器、三级换热器的流量，控制一级换热器出口处的荒煤气的温度在275～285℃，二级换热器出口处的荒煤气的温度在165～175℃，三级换热器出口处的荒煤气的温度在80～90℃。According to the above scheme, the flow rate of the first-stage heat exchanger, the second-stage heat exchanger and the third-stage heat exchanger is respectively passed through the deoxygenated water, and the temperature of the waste gas at the outlet of the first-stage heat exchanger is controlled to be between 275 and 285 °C. ℃, the temperature of the waste gas at the outlet of the secondary heat exchanger is 165-175°C, and the temperature of the waste gas at the outlet of the third-stage heat exchanger is 80-90°C.
按上述方案，在多级闪蒸罐底部分别分离出高温馏分(沥青、蒽油馏分)、中温馏分(冼油、萘油、酚油馏分)和低温馏分(轻油馏分和水)。According to the above scheme, high temperature fractions (bitumen, anthracene oil fractions), medium temperature fractions (xian oil, naphthalene oil, phenol oil fractions) and low temperature fractions (light oil fractions and water) are respectively separated at the bottom of the multi-stage flash tank.
与现有技术相比，本发明的有益效果在于：通过对焦炉荒煤气采用多段分级冷却，实现荒煤气由650～750℃冷却到80～90℃，并发生高、中和低压蒸汽，同时分离焦油高温馏分、中温馏分和轻油馏分。本发明有以下优势：(1)充分回收了荒煤气余热；(2)实现了荒煤气中馏分的粗分离；(3)多级冷凝温度可调控，克服了现有工艺中未回收高温荒煤气热量、消耗大量循环氨水的劣势。Compared with the prior art, the present invention has the beneficial effects that: by adopting multi-stage grading cooling for the waste gas of the coke oven, the waste gas is cooled from 650-750 DEG C to 80-90 DEG C, and high, medium and low pressure steam is generated, and simultaneously Separation of tar high temperature fraction, medium temperature fraction and light oil fraction. The invention has the following advantages: (1) the waste heat of the waste gas is fully recovered; (2) the rough separation of the distillate in the waste gas is realized; (3) the multi-stage condensation temperature can be regulated, which overcomes the problem that the high-temperature waste gas is not recovered in the prior art. Disadvantages of heat and consumption of a large amount of circulating ammonia.
附图说明Description of drawings
图1为本发明的焦炉荒煤气的多级冷却工艺流程以及装置图。图中，1-焦炉炭化室，2-一级换热器，3-一级闪蒸罐，4-二级换热器，5-二级闪蒸罐，6-三级换热器，7-三级闪蒸罐，8-初冷器，9-控制流量调节的温度显示控制器。Fig. 1 is the multi-stage cooling process flow and device diagram of the coke oven waste gas of the present invention. In the figure, 1- coke oven carbonization chamber, 2- primary heat exchanger, 3- primary flash tank, 4- secondary heat exchanger, 5- secondary flash tank, 6- tertiary heat exchanger, 7-Three-stage flash tank, 8-Primary cooler, 9-Temperature display controller to control flow regulation.
具体实施方式Detailed ways
为了更好地理解本发明，下面结合附图和实施例进一步阐明本发明的内容，但本发明不仅仅局限于下面的实施例。In order to better understand the present invention, the content of the present invention is further clarified below with reference to the accompanying drawings and embodiments, but the present invention is not limited to the following embodiments.
如图1所示，一种焦炉荒煤气的多级冷却装置，包括焦炉炭化室1、一级换热器2、一级闪蒸罐3、二级换热器4、二级闪蒸罐5、三级换热器6、三级闪蒸罐7、初冷器8，焦炉炭化室1的荒煤气出口与一级换热器2的荒煤气入口相连，一级换热器2的荒煤气出口与一级闪蒸罐3进料口相连，一级闪蒸罐3顶部与二级换热器4的荒煤气入口相连，二级换热器4的荒煤气出口与二级闪蒸罐5进料口相连，二级闪蒸罐5顶部与三级换热器6的荒煤气入口相连，三级换热器6的荒煤气出口与三级闪蒸罐7进料口相连，三级闪蒸罐7顶部与初冷器8入口相连。As shown in Figure 1, a multi-stage cooling device for coke oven waste gas includes a coke oven carbonization chamber 1, a primary heat exchanger 2, a primary flash tank 3, a secondary heat exchanger 4, and a secondary flash Tank 5, tertiary heat exchanger 6, tertiary flash tank 7, primary cooler 8, the waste gas outlet of coke oven carbonization chamber 1 is connected to the waste gas inlet of primary heat exchanger 2, and primary heat exchanger 2 The outlet of the waste gas is connected to the feed port of the primary flash tank 3, the top of the primary flash tank 3 is connected to the inlet of the waste gas of the secondary heat exchanger 4, and the outlet of the waste gas of the secondary heat exchanger 4 is connected to the secondary flash tank 4. The feeding port of the steaming tank 5 is connected, the top of the secondary flash tank 5 is connected with the waste gas inlet of the tertiary heat exchanger 6, and the waste gas outlet of the tertiary heat exchanger 6 is connected with the feeding port of the tertiary flash tank 7, The top of the tertiary flash tank 7 is connected to the inlet of the primary cooler 8 .
进一步地，一级换热器2、二级换热器4、三级换热器6上分别开设有除氧水的入口以及蒸汽出口；且，一级换热器2、二级换热器4、三级换热器6的除氧水入口处均安装有除氧水流量控制阀，同一个换热器除氧水入口处的除氧水流量控制阀和荒煤气出口之间均安设有控制流量调节的温度显示控制器9。Further, the first-stage heat exchanger 2, the second-stage heat exchanger 4, and the third-stage heat exchanger 6 are respectively provided with an inlet of deoxygenated water and a steam outlet; and, the first-stage heat exchanger 2, the second-stage heat exchanger 4. The deaeration water flow control valve is installed at the deaeration water inlet of the three-stage heat exchanger 6, and the deaeration water flow control valve at the deaeration water inlet of the same heat exchanger and the waste gas outlet are installed. There is a temperature display controller 9 that controls flow regulation.
实施例Example
以80万吨/年焦化厂为例，采用上述装置对荒煤气进行多级冷却工艺，具体操作步骤如下：Taking a coking plant of 800,000 tons/year as an example, the above-mentioned device is used to carry out a multi-stage cooling process for waste gas. The specific operation steps are as follows:
(1)来自焦炉炭化室1的650～750℃高温荒煤气，先经一级换热器2冷却，荒煤气温度降至275～285℃后，再经过一级闪蒸罐3进行气液分离，底部分离出高温馏分，顶部分离出的荒煤气通往二级换热器4；(1) The high-temperature waste gas at 650-750°C from the coke oven carbonization chamber 1 is first cooled by the primary heat exchanger 2, and after the temperature of the waste gas is reduced to 275-285°C, it passes through the primary flash tank 3 for gas-liquid treatment. Separation, the high temperature fraction is separated from the bottom, and the waste gas separated from the top leads to the secondary heat exchanger 4;
(2)来自一级闪蒸罐3的荒煤气经过二级换热器4冷却，荒煤气温度降至165～175℃后，再经过二级闪蒸罐5进行气液分离，底部分离出中温馏分，顶部分离出的荒煤气通往三级换热器6；(2) The waste gas from the primary flash tank 3 is cooled by the secondary heat exchanger 4, and after the temperature of the waste gas drops to 165-175 °C, the gas-liquid separation is carried out through the secondary flash tank 5, and the middle temperature is separated at the bottom. Distillate, the waste gas separated from the top leads to the three-stage heat exchanger 6;
(3)来自二级闪蒸罐5的荒煤气经过三级换热器6冷却，荒煤气温度降至80～90℃后，再经过三级闪蒸罐7进行气液分离，底部分离出轻油馏分，顶部分离出的荒煤气通往初冷器8冷却，冷却至25～35℃后送至后续工序。(3) The waste gas from the secondary flash tank 5 is cooled by the tertiary heat exchanger 6, and after the temperature of the waste gas drops to 80 to 90°C, the gas-liquid separation is carried out through the tertiary flash tank 7, and light gas is separated at the bottom. The oil fraction and the waste gas separated from the top are sent to the primary cooler 8 to be cooled, cooled to 25-35°C, and then sent to the subsequent process.
实施例中多级冷却工艺涉及的主要操作数据见表1。The main operating data involved in the multi-stage cooling process in the examples are shown in Table 1.
表1多级冷却工艺操作数据Table 1 Multi-stage cooling process operation data
对比例Comparative ratio
同样以80万吨/年焦化厂为例，采用现有的焦炉荒煤气冷却工艺，具体操作步骤如下：Also taking 800,000 tons/year coking plant as an example, the existing coke oven waste gas cooling process is adopted, and the specific operation steps are as follows:
(1)来自焦炉炭化室1的650～750℃高温荒煤气，在集气管及桥管中用压力为0.25～0.3MPa、温度为72～78℃的循环氨水通过喷头强烈喷洒，使煤气冷却到82～86℃；(1) The high-temperature waste gas at 650-750°C from the coke oven carbonization chamber 1 is strongly sprayed with circulating ammonia water with a pressure of 0.25-0.3MPa and a temperature of 72-78°C in the gas collecting pipe and the bridge pipe through the nozzle to cool the gas to 82～86℃;
(2)通往初冷器冷却，冷却至25～35℃后送至后续工序。(2) It is led to the primary cooler for cooling, cooled to 25-35°C and then sent to the subsequent process.
对比例中涉及的主要操作数据见表2。The main operating data involved in the comparative example are shown in Table 2.
表2现有工艺操作数据Table 2 Existing process operation data
经模拟计算，对比例所采用的现有工艺和本发明实施例所采用的多级冷却工艺的荒煤气及各馏分质量组成见表3。Through simulation calculation, the raw gas and the quality composition of each fraction of the existing process adopted in the comparative example and the multi-stage cooling process adopted in the embodiment of the present invention are shown in Table 3.
表3荒煤气及各馏分质量组成Table 3 The raw gas and the quality composition of each fraction
注：带*的是基于实沸点蒸馏数据和API重度表示的沥青组成，TBP表示实沸点Note: Bitumen compositions with * are based on real boiling point distillation data and API gravity, TBP means real boiling point
本实施例中，与现有工艺相比，采用多级冷却工艺后，每加工万吨煤可产生3.5MPa蒸汽2287.3吨，1.0MPa蒸汽556.3吨，0.35MPa蒸汽435.7吨。In this embodiment, compared with the prior art, after the multi-stage cooling process is adopted, 2287.3 tons of 3.5MPa steam, 556.3 tons of 1.0MPa steam, and 435.7 tons of 0.35MPa steam can be produced for every 10,000 tons of coal processed.
以上所述仅是本发明的较佳实施例，并不用以限制本发明，应当指出，对于本领域的普通技术人员来说，在不脱离本发明创造构思的前提下，还可以做出若干改进和变换，这些都属于本发明的保护范围。The above are only preferred embodiments of the present invention and are not intended to limit the present invention. It should be pointed out that for those of ordinary skill in the art, some improvements can be made without departing from the inventive concept of the present invention. and transformations, which all belong to the protection scope of the present invention.
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